DE2928210A1 - Power generator using shale oil low calorific value gas - has two=stage catalytic combustion with indirect heat exchanger between stages (NL 05.02.80) - Google Patents

Abstract

A shale oil recovery process liberates low calorific value gas in a separator. The gas flows from the separator either through a preheater or through a bypass to a first stage catalytic combustion chamber. Before entry to this combustion chamber it is preheated by indirect exchange with the combustion products of the chamber. The combustion products continue from the heat exchanger to a second catalytic combustion chamber. The products of the second chamber drive a two stage gas turbine. The turbine drives an air compressor which injects the combustion air into the gas upstream of the two combustion chambers.

Description

Device for burning gases

Low calorific value The invention relates to a gas turbine system for the generation of energy from heating or fuel gases with a low calorific value, i.e.

a calorific value of less than about 712 kcal / Nm3 (80 BTU / scf), usually in the range of 312 to 623 kcal / Nm3 (35 to 70 BTU / scf), which is an external catalytic Incinerator (hereinafter referred to as "burner"). The catalytic one Burner is catalytic in a primary or first and a secondary or second Combustion chamber divided, with a heat exchanger between the two combustion chambers is switched. In the preheater, the gas mixed with the combustion air is included low calorific value in indirect heat exchange with combustion products from the first combustion chamber before it is passed into the first combustion chamber is fed in. The turbine system can be particularly advantageous for generating energy from a gas with a low calorific value, use its combustible components Are hydrocarbons, predominantly methane.

The invention thus relates to the generation of energy from a Low calorific value gas, especially on a gas turbine system, which is used for this is designed to utilize such a gas for energy generation.

A method of increasing the capacity of the extraction of heavy High viscosity crude oils from subterranean formations is the in situ combustion process. In this process, air is injected at high pressure through an injection duct into the the underground reservoir containing heavy oil is blown. The oil in the formation becomes in the vicinity of the injection shaft after any of several known ones Methods (such as the method of US Pat. No. 3,172,472) ignited.

Air is continued to be blown in after ignition burn some of the oil in the formation and reduce the pressure in the injection shaft to increase adjacent formation areas and thereby contained in the formation Oil to a well located a reasonable distance from the injection shaft to drift. A typical in-situ incineration process is shown in U.S. Patent 2,771,951 described. The one released by the combustion of an oil fraction in the formation Heat heats the formation and the bl. In this way the viscosity of the Oil due to the high temperature, cracking or splitting of the oil and dissolving through The cracking of the low molecular weight hydrocarbons formed in the oil is severe reduced. The reduced viscosity and the pressure of the blown gases cause that the oil flows through the underground reservoir to a production well.

During the in-situ combustion processes, the combustion front moves, at which the oil in the formation burns, not in all directions with more uniformity Speed radially outwards from the injection shaft. Part of the blown air seeps in through zones of high permeability in the formation to a production well, and it there is a burn in the border areas of the seepage points or "fingers". Usually occurs long before the completion of oil production by the in-situ process a breakthrough of combustion products in the form of a smoke or exhaust gas. in the volatile constituents contained in oil or formed by cracking of the oil entrained by the blown air or the exhaust gases and carried off to the conveyor shaft. All of these factors contribute to the unevenness of the composition and the calorific value of the generated gas.

The fluids generated at the production shaft are converted into liquid petroleum products, which are withdrawn for storage or a transport line, and gaseous Separated products. The gaseous products were usually released into the atmosphere drained. The gaseous products (hereinafter referred to as "LHV gas") from the In-situ burns of heavy petroleum contain low levels of methane and C2-C6 hydrocarbons as well as nitrogen, carbon dioxide, sulfur compounds, such as hydrogen sulfide, mercaptans, or carbon oxysulfide, and sometimes a small one Amount of carbon monoxide. These gaseous products represent a fuel with little Represents calorific value, which is able to use a considerable proportion of the energy deliver the necessary to compress the to be blown into the subterranean formation by the air provided in the air inlet duct is required. Due to the lack of earth respectively.

Natural gas is important that the energy is used in production an in-situ incineration process is fully utilized. The tightening of environmental protection regulations has also imposed severe restrictions on the amounts of carbon monoxide that are present in gaseous forms Sulfur compounds very often contained in products and the hydrocarbons other than methane that are released into the atmosphere can, led.

In US Pat. No. 3,113,620, a single chute is used Described in-situ incineration process in which in an underground oil shale deposit with the help of a nuclear explosion one filled with rock trimmers or gravel Cavity is generated. An in-situ combustion process is then carried out in the cavity carried out, with the help of which the oil is removed from the rock, the drainage of the oil in a "pool" located in the bottom of the cavity and the o1 lengthways of the shaft are pressed up to the surface. The one about the oil in the in-situ incineration the gas formed by the oil poor contains a higher proportion of carbon monoxide than that formed in a conventional in-situ combustion process in an oil deposit Gas. Because the gas produced from oil shale compared to the exhaust gas of an in-situ combustion has a high concentration of carbon monoxide and hydrogen in oil deposits, the exhaust gas obtained from oil shale can sometimes be fed directly into a flame burner gas turbine used to drive an air compressor are burned.

In the publication "Power Generation from Shale Oil Process Off-Gas by J.M. McCrank and G.R. Short, presented on the occasion of the IEEE-ASME Joint Power Generation Conference in Buffalo, N.Y. (September 19-22, 1976) are the results of a technical Investigation of energy generation from the in-situ combustion of oil shale originating exhaust gas described. The blale exhaust gas is produced with the help of a combustion from the flame type to hot combustion products which are used to drive a gas turbine used, burned. As mentioned, the high carbon monoxide concentration makes it easier in the in-situ incineration or coking (retorting) of oil shale the flue gas originating from the flame combustion, however, fluctuations can occur the composition of the exhaust gas make it unsafe to maintain a stable flame.

The publication "Catalysts for Gas Turbine Combustors-Experimental Test Results "by S.M. DeCorso, S.Mumford, R.Carrubba and R.Heck, submitted at the meeting of the American Society of Mechanical Engineers (March 21-25, 1976) the combustion of a fuel known as a low calorific value gas in a laboratory-scale catalytic combustion chamber. The gas with low Calorific value is closer to synthetic coal gas with a calorific value of 1121 kcal / Nm3 (126 BTU / scf). A mixture is passed to carry out the combustion from the gas and air over the catalyst with preheating to a temperature thereby catalytic thermal combustion of that described in US Pat. No. 3,928,961 Type takes place. In this process, the mixture of fuel and Air near the catalyst surface at a temperature at which the thermal combustion occurs faster than the catalytic rate, and the surface of the catalytic converter is above the temperature of immediate self-ignition of the fuel / air mixture.

The invention relates to a system for generating energy from a low calorific value gas (LHV gas), as in an in-situ combustion process for oil production or an in-situ combustion process for coking (retorting) produced by oil shale. The LHV gas is mixed with air and brought to a temperature heated, in which the combustion of the LHV gas on contact with an oxidation catalyst is triggered. The system includes a gas turbine with an external burner, the a first stage catalytic combustion chamber and a catalytic combustion chamber a second stage with a heat exchanger connected between the combustion chambers having. The air / gas mixture is passed through the heat exchanger before it into the analytical First stage combustion chamber fed and therein by indirect heat exchange with from the catalytic combustion chamber the combustion products withdrawn from the first stage are heated. There are institutions to regulate the flow rate of the air, with the help of which the maximum Temperature rise limited and thereby excessive temperatures in the outer catalytic Combustion chamber can be avoided by a substoichiometric air flow in the burner is maintained.

In the accompanying drawings: FIG. 1 is a flow diagram of a Systems for generating energy from LHV gas from an in-situ combustion process for oil production, in which the LHV gas is used to drive a turbine sufficient pressure is provided; and FIG. 2 is a flow diagram of a system for the generation of energy from an LHV gas supplied at low pressure.

An explanation of the preferred embodiment follows.

According to Figure 1, an underground oil deposit 10, which crude oil (usually of high density and viscosity) from a production well 12 and a blow-in chute 14 located at a distance from the conveying chute. Fluids obtained from the production shaft 12 are passed through a line 16 into a Separator 18 passed, in which the LHV gas produced by the through the shaft 12 extracted liquids is separated. The fluids are from the bottom The end of the separator 18 is withdrawn into a delivery line 20, while the LHV gas from upper end of the separator 18 flows into a feed line 22. It is common expediently, the gas from the separator 18 through a suitable gas cleaning device <displayed through 24) to conduct solid particles, Catalyst poisons or other undesirable ingredients before introducing into the Separate energy generation system. It is essential for efficient operation of a gas turbine It is important that fluctuations in the mass flow of the gas to the turbine are kept to a minimum be reduced. With the aid of the flow regulator 26, a constant flow rate is achieved of LHV gas into the system.

Typical hydrocarbon concentrations in the LHV gas are in the range from about 1 to 8% by volume. The hydrocarbons consist mainly of methane; the concentration of C2-C6 hydrocarbons is usually less than 2 %. The calorific value of the LHV gas obtained from in-situ combustion in oil deposits can range from 44 to 712 kcal / Nm3 (5 to 80 BTU / scf) and usually is in the range of 312 to 623 kcal / Nm3 (35 to 70 BTU / scf), a range in which the method is particularly useful. At the hydrocarbon concentrations, which are commonly found in the LHV gas generated by in-situ combustion in oil reservoirs there may be stable combustion of methane and the other, in the case of in-situ production produced low molecular weight hydrocarbons in the absence of an oxidation catalyst cannot be achieved. Rather, stable combustion only occurs in the presence of a catalytic converter. LHV gas with a calorific value of more than 134 kcal / Nm3 (15 BTU / scf) can be burned in a catalytic burner without external heat input will. If other heat sources are available for additional preheating LHV gas with a calorific value of only 44.7 kcal / Nm3 (5 BTU / scf) can be used in catalytic Combustion chambers are oxidized.

For the most effective use possible for driving a gas turbine, with which the air used in the in-situ combustion process is compressed, the gases withdrawn from the separator 18 should, for example, have an overpressure of at least 5.3 kg / cm2 (75 psig). If the gas is a lesser Having pressure, part of the energy generated by the gas turbine is used for the Compression of the LHV gas to a level sufficient to drive a turbine Pressure is used as described with reference to FIG. The pressure in the production shafts of an in-situ incineration process in a deposit can in the range from slightly above atmospheric pressure to an excess pressure of 56 kg / cm2 (800 psig).

The pressure depends at least in part on the depth of the formation, in which the combustion takes place. Gauge pressures greater than 56 kg / cm2 (800 psig) in the production shafts could be used, but have such high Express the disadvantage that the compression of the blown into the subterranean formation Air requires high costs.

During the start-up period of the gas turbine, LHV gas will flow through the line 22 passed into a preheater 28, in which the gas to such a temperature is heated so that the LHV gas, when it comes into contact with the catalyst in a mixture with air, burns. The preheater is supplied with fuel through line 30, such as natural or natural gas, propane or liquefied petroleum gas (LPG), heated. If desired, can the combustion air for combustion in the catalytic combustion chamber the first stage (as described below) should be mixed with LHV gas before the LHV gas is passed through the preheater 28. That to the catalytic combustion chamber Ducted mixture of air and LHV gas should be used to initiate combustion a temperature of at least 2040C (4000F), preferably from 316 to 4270C (600 up to 8000F). The preheater is only used during the start-up period. After the initiation of the catalytic combustion of the first stage, the LHV gas bypasses the preheater 28 via the bypass or branch line 32, and the valves at the inlet and the outlet of the preheater are closed.

In the embodiment shown in Figure 1, LHV gas is from Preheater 28 during the start-up period or afterwards from the bypass line 32 fed into a line 34, in which it is fed through a first combustion air line 36 supplied primary combustion air is mixed. The mixture is in a Heat exchanger 38 promoted, in which it is in indirect heat exchange with hot Combustion products from the first stage catalytic combustion chamber (as described below). This brings the mixture to one temperature heated by more than 204 ° C (preferably 360 to 427 ° C) at which the combustion is triggered on contact with the catalyst. The heated mixture of LHV gas and air is passed from heat exchanger 38 via line 40 into the inlet end the primary catalytic combustion chamber 43. With a preferred Embodiment, the catalytic combustion chamber 42 has several spaced apart spaced apart permeable discs 44 that span across the combustion chamber are arranged and on which a catalytically active metal of the platinum group is deposited. The spaces 46 between the disks allow back mixing the products of the combustion of the discs, causing the development of "hot." Spots "(hot spots) in the catalyst is prevented.

The disks 44 are preferably made of a ceramic material with honeycomb structure or other configuration, which goes from the inlet side to the opposite Side of the discs has passages that allow the passage of gases in the longitudinal direction through the primary combustion chamber 42. Typical suitable catalysts are described in U.S. Patents 3,870,455 and 3,565,830. The invention is not limited to the use of a specific catalyst support or certain catalytic material. Other oxidation catalysts, such as cobalt, Lanthanum, palladium, rhodium, nickel or iron, on other types of carrier, such as granules respectively.

Grains, saddles or rings made of heat-resistant materials, can also be used.

The combustion products from the primary catalytic combustion chamber are withdrawn through line 48 at approximately 871 ° C (16000F) and into the heat exchanger 38 for the heat exchange with the LHV gas / air mixture supplied through line 36 fed in. The heat exchanger 38 is preferably tubular and jacket Heat exchangers, with the hot combustion products passing through the tubes and the LHV gas / air mixture over the outer wall of the pipes and through the space between the outer wall and the shell of the exchanger. In the preferred embodiment of the invention is secondary air for the combustion of unburned combustible Material in the combustion products withdrawn from the combustion chamber 42 in a secondary or second catalytic combustion chamber 54 by a Line 50 is fed into line 48, in which the air with the from the combustion chamber 42 withdrawn combustion products are mixed prior to introduction into the preheater 38 will. The mixing of secondary air with the effluent from the primary combustion chamber 42 usually lowers the temperature to about 93 ° C (about 2000F).

The hot flammable gas mixed with secondary air is at a Temperature from 204 to 4270C (preferably 316 to 4270C) from the heat exchanger 38 via conduit 52 into the inlet end of the secondary catalytic combustion chamber 54 transferred. The secondary catalytic combustion chamber 54 is preferred designed according to how the combustion chamber 42 is constructed. In the from the combustion chamber 42 peeled products remaining flammable compounds are in the combustion chamber 54 oxidized and withdrawn from this combustion chamber into a hot gas line 56.

By burning combustible compounds (mainly Hydrocarbons) Heat is released in the LHV gas, which is the temperature of the gases in the combustion chamber increased to a value which is the maximum permissible operating temperature of the catalytic converter does not exceed. The preferred commercially available catalysts have one maximum operating temperature of about 87100. The catalysts can also operate at higher Temperatures work, but higher temperatures shorten the life of the Catalyst. The temperature control in the catalytic combustion chamber 42 is achieved by the proportion of the combustion chamber fed Air limited so far that the temperature rise with full consumption of this The amount of air during combustion is limited to the desired range. The burn in the combustion chamber 42 always takes place with an amount of air that is smaller than the stoichiometric equivalent of the combustible substances in the LHV gas. The regulation the combustion of the LHV gas by controlling the amount supplied to the combustion chambers Amount of air to less than the stoichiometric equivalent of the combustible substances in the LHV gas means that the maximum temperature is independent of the calorific value of the LHV gas will. Fluctuations in the calorific value of the gas cannot lead to excessive catalyst temperatures to lead. Avoiding excessive temperatures by maintaining an airflow speed to the catalytic combustion chambers, which have the maximum temperature rise limit independently of the calorific value of the LHV gas, is in the US patent application Ser.No. 791 850 (filed April 28, 1977). The temperature limits in the secondary combustion chamber 54 are the same as in the primary combustion chamber 42. The maximum temperature rise in the combustion chamber 54 is limited by that the amount of air supplied through line 50 is restricted to an amount which is entirely consumed by burning combustible substances, which increase the temperature to the desired maximum.

A sudden increase in the calorific value of the LHV gas therefore does not result to excessive temperatures. Preferably each of the Combustion chambers charged with about half of the total combustion air.

Hot gas is fed into the inlet of a gas turbine via line 56 (indicated generally by 59) in which the gas is expanded to to drive the turbine and a drive shaft for generating energy in rotation to move. When the hot gas in line 56 has a temperature above the has the maximum operating temperature of the turbine, the gas is passed through a Line 57 supplied dilution air cooled to the desired temperature. In In the absence of a catalyst, the dilution air does not cause combustion of the flammable substances in the hot gas. In the case of the according to the invention shown in FIG In the embodiment, the gas turbine 59 has two sections, i.e. a first section 58 and a second section 60. Expanded gas is drawn from section 58 in the inlet of the second section 6a 'where a further expansion takes place, before venting the exhaust gas through line 62 to atmosphere.

The section 58 of the turbine drives the shaft 64 to operate a Air compressor 66 on. Compressed air from the compressor 66 is fed into a line 68, from which it flows into lines 36, 50 and 57. Another part of the compressed air from the compressor 66 is secondary air, which via a line 70 to an air compressor 72 is passed, which through the second section 60 of the gas turbine to provide is powered by air for the in-situ combustion process. From the air compressor 72 extracted air is passed via a line 74 to an air compressor 76, where they are on one for injection into formation 10 for the in situ combustion process appropriate pressure is compressed.

During operation of the device shown in FIG. 1, the flow control device 26 LHV gas withdrawing during the start-up period over a line 80 directed to a start-time turbine 82. The turbine 82 is via a shaft 84, which has a suitable coupling 86, connected to the air compressor 66. LHV gas withdrawn from turbine 82 is vented to atmosphere.

A portion of the LHV gas flow is through line 22 into the preheater 28 promoted, where it is obtained by indirect heat exchange from the combustion of a Fuel 30 derived hot combustion products is heated. Air from the compressor 66 is fed in via line 36 for mixing with the LHV gas from preheater 28 and the mixture is passed through heat exchanger 38. At the beginning of the starting period the LHV gas / air mixture in the heat exchanger is not heated.

The hot LHV gas / air mixture flows into the primary combustion chamber 42, where it first heats the catalyst to the reaction temperature and then in burns in a catalytic oxidation process.

Those withdrawn from the catalytic combustion chamber 42 are hot Combustion products are mixed with secondary air supplied via line 50 and through heat exchanger 38 in indirect heat exchange with that in the primary catalytic combustion chamber 42 led to conductive LHV gas / air mixture. That from the heat exchanger 38 withdrawing mixture of secondary air and partially incinerated air LHV gas is fed into the secondary catalytic combustion chamber via line 52 54 where an additional combustion takes place. The ones from the secondary combustion chamber The products of combustion to be withdrawn are usually at one temperature from about 8710C (16000F). This hot mixture is fed into the gas turbine via line 56 58 funded. It is usually convenient to run the gas turbine at a temperature operate from 760 to 8130c (1400 to 1550 ° F). The cooling of the hot gases in the line 56 is mixed by mixing these Gases with over the Line 57 supplied dilution air made.

After initiation of combustion in the primary combustion chamber 42 interrupts the flow of the LHV gas to the preheater 28 and conducts the LHV gas via the bypass line 32 into the line 34. The flow rate is increased of the LHV gas gradually to bring the turbine 58 to load. if the gas turbine 58 takes over the load of the compressor 66 when the clutch is released 86 to isolate start-time turbine 82 from compressor 66 and close that Valve in line 80 to cut off the flow of LHV gas to turbine 82.

The time-related fluctuations in the composition of the in-situ incineration process LHV gas formed can lead to the calorific value of the gas dropping so far that that the temperature of the products withdrawn from the secondary combustion chamber 54 is lower than the desired temperature. In order to operate as efficiently as possible To maintain the gas turbine, samples of the LHV gas are taken from line 22 taken and passed through a hydrocarbon analyzer 88 to determine the calorific value of the LHV gas. Hydrocarbon analyzers are available commercially. The analyzer 88 outputs a signal which is sent to a regulating valve 90 in a Auxiliary fuel line 92 is passed. When the calorific value of the LHV gas is on The level at which the temperature of the secondary combustion chamber drops The valve 90 ensures that the discharged products fall below the desired value for the supply of auxiliary fuel via line 92. The via lines 36 and 50 the amount of air supplied is large enough to accommodate an increase in temperature to allow sufficient combustion to the desired value, but not large enough that in the event of a sudden increase in the calorific value of the LHV gas, excessive Temperatures are generated. When the temperature in line 56 is below the desired temperature should fall, the valve in the line 50 to Increase in the secondary air by a device that responds to the temperature transmitted signal can be adjusted.

The device shown in Figure 2 is used for an initially low Pressurized LHV gas, as is common in the in-situ incineration of oil shale is won. Since the LHV gas is used for an effective turbine drive the pressure is too low, you have to compress the LHV gas to a higher pressure, which allows efficient operation of the gas turbine. Generally will an initial LHV gas overpressure for effective use in a gas turbine of at least 5.25 kg / cm2 (75 psig) is required. For this purpose there is an LHV gas compressor 100 attached to the same shaft as the compressor 66. A starting motor (starting prime mover) 102, which can be a diesel or electric motor, is for the drive of the LHV gas compressor 100 via a shaft 104. A coupling 106 allowed the decoupling of the starter motor 102 after the gas turbine 58 is used to drive the LHV gas compressor 100 and compressor 66 has been revved up.

The device shown in Figure 2 corresponds with respect to Arrangement of the air compressor 66, the outer catalytic combustion chambers 42 and 54, the heat exchanger 38 and the gas turbine 59 of the apparatus of FIG 1. Because you compress the LHV gas and the air to burn the LHV gas must, the proportion of air compressed by the compressor 66 can only be used for combustion of the LHV gas are sufficient. In this case, no air whatsoever is drawn from the compressor 66 tapped for suction by a compressor driven by section 60. The section 60 may, for example, be an electrical generator (indicated by 108) drive.

The gas turbine described here allows energy to be generated from Gas fuels with too low a calorific value for the usual gas turbine, which uses flame combustion to burn the fuel. The catalytic one Burner ensures stable combustion of fuels, their calorific values is well below the calorific value of gases that produce a stable flame, and is particularly suitable for the utilization of low calorific value Fuels whose main combustible component is methane (a difficult to burn Substance) is. The one equipped with a heat exchanger between the stages two-stage catalytic combustion chamber forms a self-contained unit, which the LHV gas / air mixture without the aid of an external heat source heated catalytic oxidation temperatures and excessive catalyst temperatures avoids. The device is particularly suitable for the recovery of gases that originate from in-situ combustion processes for oil extraction.

L e r s e i t e

Claims (16)

PATENT CLAIMS 1. Device for generating energy from one LHV gas withdrawn in situ combustion process containing a gas turbine, a air compressor driven by the gas turbine, an external combustion device for burning the LHV gas, the combustion device being a catalytic A first stage combustion chamber and a catalytic combustion chamber second stage includes a heat exchanger between the catalytic combustion chamber the first stage and the catalytic combustion chamber of the second stage Connections for conveying from the catalytic combustion chamber of the first Combustion products withdrawn through the heat exchanger to the catalytic stage Second stage combustion chamber, an LHV gas duct leading to the heat exchanger for conveying the LHV gas from the in-situ combustion process to the heat exchanger, wherein the heat exchanger for conducting the LHV gas in indirect heat exchange with the combustion products from the catalytic combustion chamber of the first Stage is constructed and arranged, one from the heat exchanger to the inlet of the catalytic Conduit means leading through the combustion chamber of the first stage and passing through the Heat exchanger with the LHV gas line device for conveying LHV gas to communicating with the first stage catalytic combustion chamber, one from the outlet the catalytic combustion chamber of the second stage leading to the gas turbine Hot gas line device for conveying hot combustion products to the Gas turbine and an air line device leading away from the air compressor Connections for the supply of compressed air to the LHV gas before the inlet to the catalytic Combustion chamber of the first stage and to that to the catalytic combustion chamber the second stage produced gas. 2. Apparatus according to claim 1, characterized in that the from Air line device leading away from the air compressor One leading to the LHV gas line first line for the supply of compressed primary combustion air to the LHV gas includes prior to its transport to the heat exchanger. 3. Apparatus according to claim 2, characterized in that the from Air line device leading away from the air compressor comprises a second line, which is arranged to bring air into that from the first catalytic combustion chamber introduced combustion products withdrawn before they enter the heat exchanger. 4. Apparatus according to claim 1 to 3, characterized in that the heat exchanger is a heat exchanger with tubes and jacket and is constructed and arranged to allow the products of combustion to pass through the pipes and passing the LHV gas between the outer surface of the tubes and the jacket will. 5. Apparatus according to claim 1 to 4, characterized by an in the hot gas line device opening the cooling air line, one in the hot gas line arranged signaling device, which reacts to the temperature of the hot gas, and a flow control device arranged in the cooling air supply line, which reacts to a signal from the signaling device installed in the hot gas line, to regulate the flow rate of the cooling air to the temperature of the gas discharged to the turbine below a predetermined maximum. 6. Apparatus according to claim 5, characterized in that the cooling gas line extends from the outlet of the compressor to the hot gas conduit means. 7. Apparatus according to claim 5 or 6, characterized in that the flow control device in the cooling air line is constructed and arranged in this way is that it increases the flow of cooling air in response to temperatures of the hot gas are higher than a predetermined temperature, and that the device an auxiliary fuel line, which connections to the delivery of auxiliary fuel in the outer burner has a device for monitoring the calorific value of the LHV gas and a flow control device in the auxiliary fuel line, which reacts to the calorific value of the LHV gas and is designed so that it The auxiliary fuel is allowed to flow if the calorific value of the LHV gas falls below a value predetermined minimum drops. 8. Apparatus according to claim 7, characterized in that the auxiliary fuel line opens into the LHV gas line installation. 9. Apparatus according to claim 6 to 8, characterized by a through the gas turbine driven second air compressor and one from the compressor outlet outgoing air line which is designed to go to the second air compressor Air in excess of the amount discharged from the compressor to the catalytic Combustion chambers and to the hot gas line is promoted. 10. Apparatus according to claim 9, characterized in that the gas turbine has two sections, each driving a separate shaft, the Air compressor by one shaft and the second air compressor by the other shaft are driven. 11. The device according to claim 3, characterized by one on the Temperature-responsive signaling device in the hot gas line and a flow control device in the second air line, which is arranged on the one in the hot gas line the temperature-reacting signaling device reacts and is designed to increase the airflow in the second duct. 12. Apparatus according to claim 1 to 11, characterized in that the catalytic combustion chambers one tubular chamber, several in the longitudinal direction spaced apart disks made of ceramic catalyst carrier, which extend across the rammers, passages, which from one side to the opposite side run to a longitudinal flow through the catalytic To allow combustion chambers, and an oxidation catalyst deposited on the discs having. 13. Apparatus according to claim 7 to 12, characterized in that the oxidation catalyst is platinum. 14. Apparatus according to claim 1 to 13, characterized in that it has a LHV gas compressor driven by the gas turbine and that the LHV gas conduit means one from the source of the LHV gas to the inlet of the LHV gas compressor line and one from the outlet of the LHV gas compressor comprises line extending to the heat exchanger. 15. Gas turbine for generating energy from LHV gas, marked by a catalytic incinerator to burn the LHV gas, 'um to generate a hot gas for driving the gas turbine, the combustion device a primary catalytic combustion chamber and a secondary catalytic combustion chamber wherein the primary and secondary combustion chambers comprise a solid oxidation catalyst have, which is so constructed and arranged in the chambers that an intimate Contact with the gas flowing through the combustion chambers as well as a small one Pressure drop in this gas will take place in a heat exchanger between the primary and secondary combustion chamber, one of the primary combustion chamber to the Heat exchanger and leading from the heat exchanger to the secondary combustion chamber Conduit device which is constructed and arranged to be removed from the primary Combustion chamber withdrawn gas into and from the heat exchanger to convey into the secondary combustion chamber a first LHV gas duct for pumping LHV gas into the heat exchanger for indirect heat exchange with the gas withdrawn from the primary combustion chamber, a second LHV gas conduit means for conveying LHV gas from the heat exchanger to the inlet of the primary combustion chamber, an air ducting device constructed and arranged to circulate air in the LHV gas before it enters the primary combustion chamber and into the gas withdrawn from the primary combustion chamber before entering the secondary Combustion chamber arrives to be fed and one from the outlet of the second combustion chamber Hot gas line leading to the gas turbine. 16. The device according to claim 1 to 15, characterized in that a LHV gas turbine driven by the gas turbine compressor and that the LHV gas line device leading to the heat exchanger has a line leading from the in-situ combustion process to the inlet of the LHV gas compressor and a conduit leading from the outlet of the LHV gas compressor to the heat exchanger includes.