PROCESS FOR SEPARATING A FLUID MIXTURE CONTAINING HYDROCARBONS AND AN ORGANIC SOLVENT

Abstract: Process for separating a fluid mixture containing hydrocarbon and an organic solvent (e.g. obtained from a dewaxing unit) by contacting said fluid mixture at elevated pressure with one side of a membrane which side is formed by a porous inorganic material which is substantially impermeable to said hydrocarbons (e.g. a capillary glass membrane) and recovering solvent (e.g. toluene and methyl ethyl ketone) from the other side of the membrane.

Description: The invention relates to a process for separating a fluid mixture containing hydrocarbons and an organic solvent. It is known to separate various hydrocarbon compounds from feed mixtures containing said compounds and a solvent by contacting the feed mixture with one side of a membrane and recovering one or more hydrocarbon compounds and/or solvent from the other (permeate) side of the membrane. Substantial energy-savings can thus be attained compared with conventional (flash) distillation- or stripping processes. In the known processes for said application polymeric dense non-porous membranes are used. A disadvantage of these membranes consists in their swelling under operating conditions which is caused by the organic solvent present in the fluid feed mixture. Moreover, such dense membranes are preferably applied as ultra-thin layers( having a thickness in the order of a few µm)in order to attain an acceptable flux through the membranes, which layers are vulnerable and need to be supported on a porous substrate. Surprisingly, it has now been found that a porous inorganic material can itself be applied as highly selective membrane in a process for separating a fluid mixture containing hydrocarbons and an organic solvent. Accordingly, the present invention provides a method for solvent recovery from oil extraction processes, comprising the steps of recovering the organic solvent from the hydrocarbon oil by contacting the mixture with one side of a membrane impermeable to hydrocarbon oil and recovering the organic solvent from the other side of the membrane, characterized in that the mixture is fed to the membrane at elevated pressure and the membrane is of capillary porous glass. It is remarked that EP-A-0143129 discloses a method for solvent recovery from oil extraction processes, comprising the steps of recovering the solvent from the hydrocarbon oil by contacting the mixture with one side of a membrane impermeable to hydrocarbons and recovering solvent from the other side of the membrane. Further, US-A-4,060,488 discloses the use of porous ceramic membranes for the separation of organic solvents from hydrocarbons. However, these citations do not relate to the separation of a fluid mixture containing hydrocarbons and an organic solvent by means of a capillary porous glass membrane. Similar remarks can be made with respect to GB-A-2,012,186. The process according to the invention is preferably carried out as a reverse osmosis - or a dialysis - process; however, it can also be carried out e.g. as a pervaporation process (in which at least part of the permeate is removed by means of evaporation from the "other side" of the membrane). In a reverse osmosis process, in which a difference in hydraulic pressure between both sides of the membrane is maintained as the driving force, flat membranes are less attractive in case the osmotic pressure is relatively high. Such flat membranes would need to be relatively thick or be supported in order to have sufficient strength to withstand the applied pressure differences, and consequently the permeate flux through flat membranes would be relatively low in this case. In contrast with flat membranes, tubular membranes, and in particular capillary membranes, can withstand relatively high pressure differences between their inner- and outer walls for a given wall thickness and are therefore preferably applied in the process according to the invention. Moreover, the inorganic membranes applied in the process according to the invention can withstand relatively high temperatures, which makes it possible to separate hot fluid mixtures therewith. The wall thickness of the aforementioned tubular (capillary) membranes may vary substantially, depending on the application thereof and the material used; a suitable wall thickness is in the range from 1 µm to 2 mm, and preferably from 5 µm to 100 µm. The diameter of tubular (e.g. capillary) membranes which are preferably applied is from 10 µm to 10 mm, and most preferably from 50 µm to 1 mm. Various porous inorganic materials can be used as membranes in the process according to the invention, provided that said material is substantially impermeable to the hydrocarbons which are to be separated from an organic solvent. Preferably, the applied membranes contain a ceramic material which can be crystalline or substantially amorphous, in particular alumina, or porous glass or quartz. The above-described porous membranes can be suitably applied as such i.e. in the form of (homogeneous) single layers. However, it is also possible to apply composite porous membranes in the process according to the invention which have been (surface) modified with e.g. hydrophobic compounds such as silicone- and/or hydrocarbon-containing compounds or which have been subjected to treatment with one or more acid- and/or alkaline-compounds. Such a modification can be carried out by any method known in the art e.g. spray-coating, impregnation, precipitation or plasma-etching. Furthermore, said porous membranes can be covered by depositing thereon a very fine dispersion of inorganic (e.g. silica) particles having a diameter of e.g. 1-100 nm. In addition, or alternatively to the modifications discussed hereinabove, the membranes can be subjected to a heat treatment, suitably carried out at temperatures from 100 °C up to the softening temperature of the porous membrane material, which treatment may be carried out at reduced, atmospheric or elevated pressure, optionally in the presence of an inert-, oxidizing- or reducing-fluid. The ready membranes as applied in the process according to the invention preferably contain pores having a substantially uniform size (i.e. the diameter in case the pores are substantially cylindrical in form) from 0.5-1000 nm, in particular from 1-100 nm, in order to attain the envisaged separation of solvent from hydrocarbons by allowing solvent molecules to permeate through the membranes, retaining hydrocarbon (e.g. oil) molecules at the feed-side of the membranes. The pressure differential applied between the one side of the membrane contacted with the fluid feed mixture (the feed-side) and the other (permeate) side is suitably from 2-200 bar, and preferably from 10-80 bar. The temperature at which the present process is carried out may vary within a wide range and is not critical as long as the applied membranes can withstand the operating conditions. A fluid feed temperature from -40 °C to +400 °C is suitable in most cases, whereas a temperature from -20 °C to +300 °C is preferred. The process according to the invention is well suited for applications in which a fluid feed mixture containing as the organic solvent an aromatic- and a polar aliphatic-solvent is available. This is the case when hydrocarbon oils have been subjected to a solvent dewaxing treatment with said organic solvent(s). During such a treatment usually a toluene/methyl ethyl ketone solvent mixture is added to a wax-containing oil, followed by removing wax (e.g. by means of filtration). The solvents are usually recovered from the dewaxed hydrocarbon oil in a conventional flashing process with high energy consumption. With the process according to the invention it is possible to reduce said energy consumption considerably by recovering a major portion, or even substantially all, of the solvents via membranes and separating only the remaining portion of solvents, if any, by conventional means. The aromatic solvent: polar aliphatic solvent weight ratio in the feed mixture is suitably from 0.1-10, and preferably from 0.5-5. Other preferred applications of the process according to the invention are the separation of furfural from furfural/lubricating oil mixtures obtained from a furfural extraction process, and the separation of solvents (e.g. liquid propane and/or butane) from deasphalted hydrocarbon oil residue fractions. The organic solvent: hydrocarbons weight ratio in the feed mixture is suitably from 0.5-5, and preferably from 1-3. An organic solvent: hydrocarbons weight ratio of less than 0.5 usually has a negative influence on the present process because the solvent flux through the membranes then becomes unacceptably low at a given pressure differential between both sides of the membranes due to the high osmotic pressures which reduce the driving force. Because of the above-mentioned influence of the organic solvent: hydrocarbons weight ratio in the feed mixture on the solvents flux it is preferred to carry out the process according to the invention with a number of membrane units in a series-flow set-up, thus increasing the oil-content of the feed mixture gradually in subsequent membrane units and maintaining a relatively high solvents ratio in the upstream membrane units. This way the total required membrane area can be reduced in comparison with a single-stage membrane separation process for a given quantity of feed mixture to be treated. In order to avoid, or at least reduce fouling and concentration polarization of the membranes, the feed mixture is preferably passed along one side of at least one following membrane. In order to prevent concentration polarization even better, part of the feed mixture which has been passed along one side of a membrane can be recirculated by reintroducing said part into the feed mixture to be passed along said side of the same membrane. The invention further relates to hydrocarbons whenever obtained by a separation process as described hereinbefore. The following Example illustrates the invention. EXAMPLE A liquid feed mixture containing equal amounts by weight of dewaxed bright stock (hydrocarbon oil obtained by dewaxing a vacuum residue), methyl ethyl ketone and toluene was contacted at a pressure of 19 bar abs. and a temperature of 20 °C with the inner channels of porous capillary glass membranes having a pore size of 3 nm, an outer diameter of 460 µm and a wall thickness of 45 µm. A selectivity (α) of 20 was attained, defined as: wherein X = concentration in the feed mixture and Y = concentration in the permeate.

Claims: A method for solvent recovery from oil extraction processes, comprising the steps of recovering the organic solvent from the hydrocarbon oil by contacting the mixture with one side of a membrane impermeable to hydrocarbon oil and recovering the organic solvent from the other side of the membrane, characterized in that the mixture is fed to the membrane at elevated pressure and the membrane is of capillary porous glass. The process as claimed in claim 1 characterized in that the pore size of the membrane is from 0.5-1000 nm, preferably from 1-100 nm. The process as claimed in claim 1 or 2 characterized in that the pressure differential applied between the one side of the membrane contacted with the fluid mixture and the other side is from 2-200 bar, preferably from 10-80 bar. The process as claimed in any one of claims 1-3 characterized in that the organic solvent comprises an aromatic- and a polar aliphatic-solvent. The process as claimed in any one of claims 1-4 characterized in that the feed mixture has been obtained by subjecting a hydrocarbon oil to a dewaxing treatment with the organic solvent. The process as claimed in any one of claims 1-5 characterized in that the organic solvent hydrocarbons weight ratio in the feed mixture is from 0.5-5, and preferably from 1-3.

Inventors: BITTER, JOHAN GEORGE ALBERT, HAAN, JOHANNES PIETER
Applicants: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.
Application year: 1987
Main classification: B01D61
IPC codes: C07C1, C07C67, C10G21, B01D61, C10G31, C07C7