Method for preparing fuel mixtures for torches and burners

#This invention relates to a method of obtaining a fuel mixture for torches and burners used for welding and cutting.

#For more than 50 years, it has been conventional to use acetylene as the fuel for torches and burners for welding and cutting apparatus. The nature of acetylene, however, is such that it is dangerous to store it when compressed and on its own, and it is conventionally stored, after being compressed and dissolved in a solvent such as acetone, in a porous material. Under these conditions the amount of acetylene which can be stored or transported is low relative to the weight of the container and of its contents. Methods have been proposed for the transport and storage of acetylene in liquid form, but pure liquid acetylene is not used, owing to the risk of explosion and the difficulty of handling it.

#It has recently been proposed to use acetylene mixtures, which avoid the risk of explosion and can give a sufficiently high combustion temperature for welding and oxygen cutting. These liquid fuel mixtures, which contain from 60 to 10 mols% acetylene and from 40 to 90 mols % ethylene, can be stored or transported at normal temperature in compressed form at a pressure of about 80 kg/cm.sup.2. When the liquid mixture is stored at this relatively high pressure, it has to be supplied in cylinders, usually of low capacity, which means that the cost of using it is relatively high and it cannot be distributed on a large scale by a pipe system.

#For a better understanding of the invention and to show how the same may be carried into effect, reference will now be made, by way of example, to the accompanying drawing which shows an installation for preparing a fuel mixture by the method of the invention.

#The installation comprises a tank 1 for storing ethylene, a valve 2 on a pipe 3 for introducing ethylene into a boiler 4 in which the ethylene is vaporised by counter-current cold exchange with a fraction of the fuel mixture (which has already been prepared), after which the gaseous ethylene is heated in a heat exchanger 5 in counter-current and with cold exchange with said fraction of the gaseous fuel mixture. After being vaporised and heated to a temperature in the range of from -25.degree. C. to +20.degree. C. in said boiler and heat exchanger, ethylene is introduced via pipe 3 into a mixing unit 6 which comprises means for introducing acetylene in controlled proportions, the acetylene arriving at the mixing unit via a pipe 7. The gaseous fuel mixture thus produced is withdrawn from the mixing unit via a pipe 8 and conveyed to a compressor 9 in which it is compressed before being cooled in a cooler 10. A multi-way valve 11 is used to bleed off a fraction of the fuel mixture in gaseous form and under a slight pressure, so that it can be distributed by a pipe 12 and via an expansion valve 13. The other fraction of the fuel mixture is bled off via a pipe 14 and is conveyed to a drier 15. This other fraction enters the heat exchanger 5 at ambient temperature and is cooled therein and also in boiler 4 by cold exchange with the cold ethylene, and is then cooled in a liquid nitrogencooled condenser 16 (for starting or for safety purposes), the nitrogen coming from tank 17. The liquid, cold fuel mixture is stored under a slight pressure in a storage tank, provided with withdrawal means. The liquid fuel mixture can be conveyed by a pipe 19, via a pump 20 and a valve 21, to a tanker. If there is a considerable demand for a gaseous fuel mixture, a fraction thereof can be withdrawn via a pipe 22, under the control of a valve 23. After travelling through exchanger 24, the fraction of the gaseous fuel mixture is combined with the first fraction of the same mixture flowing in pipe 12.

#The invention is further illustrated by the following specific Example.

#The liquid ethylene used for the process is at a temperature of -100.degree. C. and a pressure of 1.4 bara. On leaving the boiler 4 after being vaporised, it is at a temperature of -90.degree. C. and at a pressure of 1.4 bara. After travelling through the heat exchanger 5 it is at a temperature of -26.degree. C. and a pressure of 1.15 bara and, in gaseous form, enters the mixing unit 6 at a flow rate of 100 m.sup.3 /h at -15.degree. C. Acetylene at 20.degree. C. and atmospheric pressure is admixed with the ethylene at the rate of 20 m.sup.3 /h at -15.degree. C. The fuel mixture produced in the mixing unit is withdrawn at a temperature of 15.degree. C. and at a pressure of 1.05 bara. It is then compressed in the compressor 9 to 5 bara, then cooled in the cooler 10 to ambient temperature, i.e. approx. 20.degree. C. The fraction of the mixture for distribution in gaseous form is withdrawn at a pressure of 2.5 bara. The second fraction of the gaseous mixture is dried in the dryer 15 to less than 100 ppm moisture. The dry fuel mixture, which is at a pressure of 4.8 bara and a temperature of 20.degree. C., is cooled to -60.degree. C. in the heat exchanger by cold exchange with ethylene. At the outlet of boiler 4, the temperature drops to -75.degree. C. and the pressure is 4.2 bara. After the liquid fuel mixture has travelled through the liquid-nitrogen condenser 16, its temperature is -80.degree. C. and it is at a pressure of 3.9 bara. The liquid mixture is stored under these temperature and pressure conditions, and most of it is withdrawn for filling thermally super-insulated tankers. However, part of the liquid is withdrawn and sent through an expansion valve whereat it suffers a pressure drop from 3.9 to 2.5 bara; thereafter it is heated to approx. 20.degree. C. in the exchanger 24 and combined with the mixture distributed in gaseous form.