CONTINUOUS PROCESS FOR THE REMOVAL OF SULPHUR DIOXIDE FROM WASTE GASES, AND HYDROGEN AND SULPHURIC ACID PRODUCED THEREBY

Abstract: A continuous process for the removal of SO₂ from a stream of waste gases comprising contacting the waste gas stream with a stream containing water and bromine. Preferably the resulting hydrobromic acid is electrolysed to produce hydrogen and bromine; which bromine is then recycled to the contacting stream.

Description: "CONTINUOUS PROCESS FOR THE REMOVAL OF SO FROM WASTE GASES, AND HYDROGEN AND SULPHURIC ACID PRODUCED THEREBY " The invention is concerned with a process for the removal of SO, from waste gases. It is known that most fossil fuels, such as heavy fuel oil and coal, contain considerable quantities of sulphur. This gives rise to the emission of significant quantities of sulphur dioxide in the combustion product gases. Sulphur dioxide, however, is a very harmful agent: 3 daily averages above 300 microgram/m3 (0.11 n m) are already considered hazardous to human health. Consequently, current standards of protection of the environment call for the removal of the majority of the sulphur dioxide from the combustion waste gases, before those gases are vented into the atmosphere. The known processes to remove S02 from waste gases can be classified into two general categories; those processes in which the sulphur is disposed of as waste (throw-away produ-t systems) and processes in which the sulphur product, in the form of, e.g. elemental sulphur or sulphuric acid, is marketed (saleable product processes). The following commercially-offered throw-away and saleable product systems are considered the most important for near future (about 1985): Throw-away : lime scrubbing, limestone scrubbing and double alkali process; Saleable product : magnesium oxide scrubbing and sodium sulphate scrubbing (Wellmann-Lord Process). The drawbacks of the existing processes are mainly of a practical and economical nature: The throw-away processes produce a very impressive amount of valueless material which must be disposed of. To give an example, a 600 MWe power station using coal containing 2.5% of S produces annually approximately 300 000 tons of sludge. Disposal of these huge amounts cleats a considerable practical and financial problem for the power-producing utilities. On the other hand, the saleable product processes are expensive, especially with regard to investment costs. Moreover, they generally produce sulphuric acid in a rather dilute form. This fact either requires additional (expensive) concentration procedures or gives rise to difficulties in marketing the product. The present invention seeks to overcome these drawbacks. Processes are also known for removing impurities, such as sulphur dioxide, from gas streams using chlorine in the presence of water (see, for example, United Kingdom Patent Specification Nos.603735, 901630, 1399214, 1474626 and 1496143); but it has not been suggested that there are any advantages in using bromine rather than chlorine as the oxidising agent. In United Kingdom Patent Specification No. 1399214, bromine is mentioned as one of many possible oxidising agents which may be used in the particular apparatus disclosed and claimed in that specification, but again no particular advantage has been suggested for its use in removing sulphur dioxide. Furthermore, the specification teaches the use of a semi-permeable membrane to separate the gas to b# purified from the oxidising solution so that no direct contact can take place between the two phases. In accordance with the present invention there is provided a continuous process for the removal of S02 from a stream of waste gases comprising contacting the waste gas stream with a stream containing water and bromine. ¯In the preferred embaBrEnt of the invention, the process comprises treating the S02-containing waste gases with water and bromine separating the resulting sulphuric acid from the resulting hydrobromic acid and electrolyzing this hydrobromic acid to obtain hydrogen and bromine, which bromine can be recycled to remove SO, from the waste gases. This process is based on the well known reaction: SO, + Br2 + 2 H20 ) 2 HBr + H2S04 The above equilibrium is completely shifted towards the right when the applied aqueous solutions are dilute (less than 50 wt % of sulphuric acid), whereas observed reaction rates are very fast. Therefore, when a 502 containing gas is contacted with an aqueous solution containing bromine, hydrogen bromide and sulphuric acid, the reaction proceeds rapidly and to completion. Even with very small concentrations of sulphur dioxide (0-3000 ppm volume) satisfactory reaction rates and S02 removal are obtained. Suitable boundary conditions for the concentrations of the various compounds in the aqueous phase for this reaction are: Sulphuric acid: between 0 and 50 wt %, Hydrogen bromide: between 5 and 40 wt %, Bromine: between 0 and 10 wt %. The bromine required for the removal of SO, from waste gases can be regenerated from hydrogen bromide by electrolysis of the latter: 2 HBr i H2 + Br2 This reaction thus produces hydrogen, which can be, considered a very valuable and saleable product. The electrolysis is carried out by passing the solution used for the SO 2-removal reaction through an electrolytic cell, where low voltages (probably below 1 Volt) can be applied to obtain the required reaction. Hydrogen is formed in the gaseous phase and can easily be purified from traces of bromine, whereas practically all the formed bromine remains dissolved in the circulating liquid. The procesed process is finally completed with the concentration of sulphuric acid and the removal of HBr from the aqueous solution. This necessary step can advantageously be performed by contacting the incoming waste gas (which usually has a temperature of 150 to 2000C) with a small side-stream of the aqueous solution coming from the S02 removal reactor. Here the HBr present is completely evaporated from the solution together with a large part of the water from the solution. In this way it is possible to produce a concentrated sulphuric acid product. It is particularly interesting that in this operation no additional heat is necessary: the contact tower can operate fully adiabatically. A block diagram of the proposed process is given in the accompanying drawing. This is an example of a small pilot plant, treating 2150 cubic meters per hour of a typical combustion gas coming from a fuel oil or coal burning furnace. This can be considered a typical example of a possible application which may serve for further elucidation of the process principles. 3 The incoming waste gas 1 contains 4.0 g/m S.T.P. (S.T.P. means Standard Temperature and Pressure, i.e. room temperature and atmospheric pressure.) of sulphur dioxide (1500-ppm volume). It has a dew point of 410C, corresponding with a water content of 59 g/m3 S.T.P. and enters the process at a temperature of 1850 C. This gas strea enters the adiabatic evaporator 2. To this reactor is also fed a solution 3, containing 25 wt % sulphuric acid and 20 wt e hydrobromic acid in water. This solution comes from the S02-removal reactor at a flow rate of 47.4 kg/h. The two streams 2 and 3 are intensively mixed in a suitable type of apparatus, such as a spray column or a concurrent downflow contactor with liquid -recycle, for instance. During this operation, all of the HBr passes into the vapour phase together with a large part of the water from the incoming solution 3. The final liquid product 4 is a solution of sulphuric acid in water, containing 85 wt % HSO, which is a valuable and saleable product. 13.9 kg/hr of the product are obtained. During the operation the temperature of the gas stream drops to l550C and the exit gas 5 contains now, 3 besides the original sulphur dioxide, also 4.4 g/m of HBr. Its water content has increased to 70 g/m3 S.T.P., a dew point of 44.50C. This gas stream now passes to the S02-removal reactor 6 which may be a downward flow, concurrentlyoperated, packed column 1 meter in diameter and 3 meters in height. In this unit, the gas stream 5 is contacted with a solution 7 coming from the electrolytic cell 8 containing 2 wt % of bromine. The HBr present in the gas phase is dissolved in the liquid, whereas the sulphur dioxide reacts with bromine and water to form HBr and H2SO4. Both these products remain quantitatively in the liquid phase. The product gas 9, then, is essentially free from HBr, since the partial pressure of hydrogen bromide in the gas phase in equilibrium with the liquid phase composition is of the order of 10 4 mm Hg. 2150 m3/h of product gas is produced with an S02 content 3 of 0.3 g/m at 500C. Thus 93% of the S02 in the waste gas has been removed. The in-complete removal of the sulphur dioxide is due to the fact that the bromine generated by the electrolytic cell 8 is intentionally kept in stoichiometric deficiency with respect to the SO, entering with the gas phase. This is done to avoid possible bromine losses. Obviously, the SO 2-removal efficiency can further be raised by increasing the amount of bromine produced by the electrolytic cell. The temperature of the SO- removal reactor must be controlled in such a way that the leaving gas 9 has a 3 humidity of 57 g/m S.T.P. water vapour content. By doing so, the water needed for the reaction is taken from the humidity of the incoming flue gases an no additional water supply is necessary. The required reaction temperature will be between 45 and 50cm. The bulk of the liquid phase 10 leaving the reactor 6 is passed to the electrolytic cell 8. The flow rate into the cell is 1000 kg/h. Here a part of the HBr is converted into hydrogen and bromine, producing a solution containing 18 wt % of hydrogen bromide and 2 wt % or bromide. A small stream 3 (47.4 kg/h) of liquid goes to the evaporator 2, removing the formed sulphuric acid from the reactor and transporting it to the final product 4. The electrolytic cell 8 may very well consist of 2 graphite electrodes; the total surface being about 3 rn A basic cell voltage of approximately 1 Volt is applied between the electrodes, causing a current flow of approximately 7.5 kA. The energy efficiency in such a cell will be about 90%; giving rise to a total hydrogen 3 production rate of 3.0 m /h at S.T.P. Bromine is produced at a rate of 20 kg/h. The invention offers several advantages when compared to the current processes. It does not produce the huge amounts of valueless, disposable products, as are produced in the current throw-away processes, such as lime and limestone scrubbing. The su;huric acid produced is of high concentration and is directly produced in one single reaction step. No additional thermal regeneration steps are required, as proves to be necessary in the Wellmann-Lord and magnesium oxide processes. The internal regeneration of bromine by HBr electrolysis produces a considerable stream of pure hydrogen, which is a very valuable bye-product of the process. No solid materials or slurries are required as reactants. Reaction rates are high and will probably only be diffusion controlled, so that reactors of relatively small dimensions can be utilized.

Claims: Claims: 1. A continuous process for the removal of SO, from a stream of waste gases comprising contacting the waste gas stream with a stream containing water and bromine. 2. A process as claimed in claim 1 wherein the resulting sulphuric acid and hydrobromic acid are separated. 3. A process as claimed in claim 1 or claim 2 wherein the resulting hydrobromic acid is electrolyzed to produce hydrogen and bromine. 4. A process as claimed in claim 3 wherein the resulting bromine is recycled to the contacting stream. 5. A process as claimed in any one of the preceding claims wherein the contacting stream contains: Sulphuric acid: between 0 and 50 wt %, Hydrogen bromide: between 5 and 40 wt %, Bromine: between 0 and 10 wt %. 6. Hydrogen when produced in accordance with a process as claimed in claim 3. 7. Sulphuric acid when produced in accordance with a process as claimed in claim 2.

Inventors: DE BENI, GIANFRANCO, LANGENKAMP, HEINRICH, VAN VELZEN, DANIEL
Applicants: EUROPEAN ATOMIC ENERGY COMMUNITY (EURATOM)
Application year: 1979
Main classification: B01D53
IPC codes: C01B17, B01D53, C25B1