for the following exemplary embodiments , a special type of burner was selected , i . e . the previously already more thoroughly discussed pore burner 1 , which presents particular benefits in comparison with other burner types . the essential characteristic of the invention consists in that the flame is cooled by supply of an additional gas to the fuel / oxidant mixture , which can be realized with respect to all conceivable burner types . therefore , the description of exemplary embodiments which follows is not to be regarded as limitation on the basis of pore burner 1 alone . a general exemplary embodiment of a pore burner 1 for chemical processes is represented in fig1 . the housing of pore burner 1 consists of artificial resin - impregnated graphite and is traversed by cooling channels 2 , which transport cooling agents , for example , cooling water . in addition , two zones are depicted , zone a and c , defined by sphere - shaped filling bodies . zone c acts as combustion zone in which the flame develops . by appropriate dimensioning , ignition is avoided in zone a . the combustion zone c is filled for that purpose with larger sphere - shaped filling bodies 3 — zone a , on the other hand , is filled with smaller sphere - shaped filling bodies 3 ′. in a lower section are gas inlet channels 6 , which issue tangentially into the pre - mix chamber 5 , as is depicted , in detail , in fig3 a . due to the tangential supply , effective mixing takes place by means of swirling . in addition , a condensate outlet 7 is provided at the pre - mix chamber whose position — depending upon the installation position of burner 1 , is established in downward direction , so that the condensate is able to run off . the pre - mix chamber 5 can , furthermore , contain , depending upon need , static mixing elements 10 , as they can be seen in detail in fig1 a , as segment of fig1 . in order to simplify cleaning , the lower portion 4 is detachably attached at the housing of pore burner 1 by means of an attachment device 8 . in order to achieve an essentially adiabatic combustion , the combustion chamber c is thermally screened off against the cooled housing wall of the pore burner 1 by means of a ceramic insulation 9 . at the gas exit 11 , the combustion chamber c is topped with a grate 12 , which prevents that filling bodies can fall out of the pore burner 1 in case of other than vertical installation . another grate 13 between the zones a and c prevents that small filling bodies of zone a are blown into the intermediate spaces of the filling bodies of zone c . grate 14 , which can likewise be seen in fig1 , separates the pre - mix chamber 5 from zone a . in the combustion chamber wall of pore burner 1 and the isolation 9 , a continuous opening 15 is provided for measuring the temperature and an opening 16 in order to ignite the mixture . in order to lower the flame temperature to less than maximum temperature , at which temperature the spheres will not melt , an additional gas is supplied to the pre - mix chamber , such as water vapor , exhaust gas from the combustion or another type of gas . fig2 depicts a pore burner , which operates in the same manner as the burner of fig1 . in contrast to the burner of fig1 , no pre - mix chamber is provided here . the gases are introduced by means of lines 6 directly into zone a . pervasion of spaces between the spheres 3 ′ leads to highly uniform distribution , so that the gases introduced into zone a via supply line 6 mix with one another very well . as is apparent from fig2 a , the supply lines 6 present a multitude of holes , which mainly take care of uniform distribution at the bottom of the pore burner and , if dimensioned sufficiently small , can prevent flame backfire into lines 6 . in addition , two of the combustion gases , for example cl 2 and h 2 are carried in separate lines 6 , which are laterally at a distance from zone a and are introduced from opposite sides , so that no accidental mixing can take place in the proximity of the principal supply , for example due to leaks , which might lead to an explosion , somewhere . fig3 depicts another specific embodiment , in which the combustion gases themselves provide for cooling and corresponding heat transfer . the hydrogen is initially conducted for that purpose through cooling channels of the combustion chamber wall of pore burner 1 , before entering through an inlet channel 6 in the under - section 4 into the pre - mix chamber , as is indicated by arrows on the left and right hand side of fig3 . the chlorine enters through another gas inlet channel 6 . an outside gas is blown into the pre - mix chamber 5 through additional gas inlet channels 6 , as can be seen in detail in fig4 a . in this specific embodiment , the design of the insulation should be adapted to the heat absorption capability of the hydrogen . in this example , the combustion chamber c is filled with a structured packing 3 ″, by means of which there is improvement in the mixing of the reaction partners compared with the sphere packing according to fig1 . such packings 3 ″ are particularly appropriate for those instances where no solid substances are contained in the gases , such as carbon black . fig4 depicts another exemplary embodiment of a pore burner 1 , which is encased by a graphite wall , which is surrounded by a water - cooled casing 17 of steel . the graphite wall of the pore burner 1 does not need , in this case , any interior cooling channels because of the high thermal conductivity of carbon . the cooling water enters at the stub 18 into the casing space 19 of the steel casing 17 and leaves same again through a stub 20 . the pore burner represented in fig4 is equipped with ceramic fill body rings 3 ′″ ( to demonstrate another design relative to zone 5 )— said rings present a cylindrical shape with inner structures . by means of such structures , the surface is raised , mainly relative to the example of fig1 . fig4 a depicts , by way of example , the location of the entry stub 6 for the pre - mix chamber 5 . combustion gases and inert gases are preferably supplied to peripherally consecutive entry stubs 6 , in order to lower the flame velocity of the mixtures , for example hydrogen at 6 ′, chlorine at 6 ″ and circulating gases at 6 ′″. condensates can exit from the pre - mix chamber at stub 7 . fig5 shows a pore burner 1 for after - combustion of chlorine - containing gases . it differs from the in fig1 described specific embodiment by a modified pre - mix chamber 5 , into which issues a generously dimensioned gas entry channel 21 , through which flow the pre - mixed gases , air as oxidant and fuel . a gas inlet pipe 22 , through which is conducted the subsequently to be combusted exhaust gas , also projects into the pre - mix chamber 5 . the gas inlet pipe 22 is fitted with borings 23 at its casing surface , through which the exhaust gas to be subsequently combusted , enters into the pre - mix chamber 5 and mixes with the fuel gas stream which flows around the pipe . the condensate outlet 7 is in this case laterally arranged , in contrast to the representations of fig1 - 3 . the pre - mix chamber 5 widens below zone a to the same cross - section as the one of zone c . said widening affords an increase in the possible gas load of the burner . fig6 depicts a simplified diagram of a facility for the production of hydrochloric acid , into which is integrated a pore burner 1 , for example of the type according to fig3 . the combustion gases , hydrogen and chlorine are in this arrangement fed into a pore burner 1 via supply lines 25 , 26 . the reaction products get from the pore burner via a line 27 into a heat exchanger 28 for cool - down . the heat exchanger can be cooled , for example , with cooling water . alternatively , however , heat utilization is also possible in that hot water or low pressure steam is generated there for further utilization . from the cooled - down gases exiting from the heat exchanger , a portion is segregated via a line 29 and passed to the fuel / oxidant mixture via a supply line 30 in front of the burner . temperature regulation takes place by means of a corresponding measuring station 31 and a temperature - controlled valve 32 . the other portion of the gases gets , via a line 33 , into a drop foil absorber 34 , for example , in which hydrochloric gas is absorbed in water or diluted muriatic acid and withdrawn from the stub 35 . the washer , designed here as drop foil absorber 34 , can be operated by direct current , as represented , or also by opposite current . the non - absorbable and insignificant portions of hydrochloric gas then get into an after - wash unit 36 , in which the remaining portions of hydrochloric gas are washed out by means of fresh water supplied via line 37 . the washing water enriched with hydrochloric gas is beneficially utilized as absorption liquid for the absorption unit and returned for that reason . fig7 depicts another schematic representation of a facility which can be employed , for example , for post - combustion of chlorine - containing compounds and exhaust gases having low chlorine contents from other fixtures or components of fixtures . an exhaust gas with chlorine - containing components supplied via a line 40 is post - combusted in a pore burner 1 by means of a support flame from natural gas and air supplied via lines 38 and 39 . the combustion temperature of the pore burner 1 is controlled in this example with the aid of additional air via a valve 41 , if the cooling effect of the subsequently to be combusted gas supplied via line 40 is insufficient , or if it has a heating value that needs to be considered . needless to say , other gases , for example inert gases or steam , can also be supplied for regulation of temperature , if the extreme parameters so require . if the combustion temperature is lower than the specified target value , the heat output needs to be increased by supply of natural gas . the exhaust gases can be passed to an exhaust heat exploitation unit in a heat exchanger not represented here , or they can be quenched directly as is frequently the case with small facilities . after quenching , the chilled gases reach a washer 42 , in which the exhaust gases are initially washed with circulating fluid , then with fresh water supplied via line 37 . a portion of the wash water is subjected to further processing . this , however , is not indicated in the drawing . the purified exhaust gas escapes from a line 43 , while diluted hydrochloric acid can be removed via a line 44 . the particular benefits of a pore burner 1 in such plants are based on its outstanding capability of regulating the combustion temperature and in its combustion stability . the stabilizing effect of the hot ceramic materials in zone c has a positive effect upon any sudden changes in the composition of the subsequently to be combusted exhaust gas . the other combustion parameters , such as natural gas and air requirement for maintaining the target temperature in the combustion zone can quickly be adapted without interrupting the combustion . combustion temperatures of up to 1600 ° c . are possible with commercially available ceramic oxide aggregate . hydrochloric acid was produced from hydrogen ( 1 . 12 m 3 / h ) and chlorine ( 1 . 09 m 3 / h ) with a pore burner 1 according to fig1 . in a process - engineered pilot plant according to fig5 . a stream of inert gas stream was blown in as added gas for lowering the flame temperature , also 0 . 73 kg / h of steam was added into the pre - mix chamber . with a stoichiometric hydrogen surplus of 3 %, a free chlorine contents of less than 3 % was ascertained in the 30 % ( by weight ) hydrochloric acid , which was produced by combustion . an exhaust gas containing methyl - chloride was subjected to post - combustion in a pore burner 1 according to fig5 , in a plant according to fig7 , in a support flame of 0 . 17 m 3 natural gas and 1 . 54 m 3 / h air . a post - combustion gas with approximately 0 . 1 % methyl chloride in air was introduced as exhaust gas with 0 . 35 m 3 / h . the temperature of the exhaust gas escaping from the pore burner was at approximately 1100 ° c . the contents of methyl chloride in the exhaust gas was less than 12 ppm . the following results were obtained in a test using a plant according to fig6 and a pore burner according to fig1 : combustion of 0 . 12 m 3 / h chlorine with 0 . 2 m 3 / h natural gas ( methane ) and 2 . 8 m 3 / h air . hydrochloric acid ( 30 %) free from carbon black was produced . contents of carbon mono - oxide was smaller than 0 . 5 %. by - products such as polychlorinated dioxins and furans could not be ascertained in the acid nor in the exhaust gas . chlorine contents in the acid was less than 50 ppm . subject to unfavorable parameters , the exhaust gas with high air excess could once more be subjected to after - combustion in a device according to fig5 . in addition , tests were performed at greatly reduced combustion chamber temperature in a burner according to fig1 . using 1 . 06 m 3 / h hydrogen , 1 . 04 m 3 / h chlorine and 1 . 02 kg / h steam , even with low combustion chamber temperature of approx . 600 ° c ., there resulted only low chlorine contents in the obtained acid of less than 3 ppm . as demonstrated by these examples , the above named burner types make it possible to basically execute , in simple fashion , highly exothermal chemical reactions , in low volume scale as well as in adiabatic manner . safety provisions can easily be maintained . thus , the burner type described here proves itself in all requirements vastly superior for highly exothermal chemical reactions when compared with the traditional burners .