PROCESS FOR THE GENERATION OF POWER AND THE PREPARATION OF LIQUID HYDROCARBONS

Abstract: Power is generated and liquid hydrocarbons are pre­ pared in a process in which less than 70%v of a mixture of carbon monoxide and hydrogen is converted by means of a hydrocarbon synthesis carried out above 300°C. From the reaction product are separated a liquid fraction which comprises the desired hydrocarbons and a gaseous fraction which, in addition to unconverted carbon monoxide and hydrogen, comprises light hydrocarbons formed during the synthesis and which latter fraction is combusted. The combustion gas is used for generating power in a gas turbine. High pressure steam is produced from water by pre-heating, vaporization and superheating by using the hot exit gas of the gas turbine. At least part of the reaction heat from the hydrocarbon synthesis is used in the vaporization stage of the steam production. The high-pressure steam is used for generating power in a steam turbine.

Description: PROCESS FOR THE GENERATION OF POWER AND THE PREPARATION OF LIQUID HYDROCARBONS The invention relates to a process in which, starting from a mixture of carbon monoxide and hydrogen, power is generated by means of a combined gas turbine-steam turbine system and, in addition, liquid hydrocarbons are prepared by means of a hightemperature hydrocarbon synthesis and in which both exhaust beat and gaseous by-products obtained in the hydrocarbon synthesis are used in the generation of power. An attractive method of generating poeer from a variety of gaseous and liquid fuels comprises the conversion by combustion of the fuels into gas having a high pressure and a high tempera- ture, which is used to generate power in a combined gas turbine steam turbine system. In short the principle of the working of a catbined gas turbine-steam turbine system is to the effect that the combustion gases are expanded in a gas turbine, thus generating power and that the hot exhaust gas from the gas turbine is used for the production of high-pressure steam which, by expansion in a steam turbine, produces an additional quantity of power. The combined gas turbine-steam turbine system may be used very suitably for the generation of power fran coal by gasifying the coal, purifying and then combusting the synthesis gas obtained and generating power from the combustion gases by means of the combined gas turbine-steam turbine system. With a view to controlling air pollution due to sulphur emissions the aforedescribed method of energy generating fran coal may be regarded as an attractive alternative. to the conventional coal-fired power plant equipped with flue gas cleaning facilities. As regards the generation of power by using a combined gas turbine-steam turbine system, the following should be noted. Amcng the various possibilities of combining the two turbines what is called the wrecuperation scheme" is the preferred option for ccolverting a clean fuel gas into power, since this scheme turns to optimum account the clean burning praperties of the fuel, the relatively low capital cost per unit of power of gas turbines and the possibilities offered by advanced gas turbine technology. In this scheme the power is mainly generated in the gas turbine and the waste heat of the gas turbine is recuperated in a relatively simple way by using heat exchange to utilize the exhaust gases for the production of steam. In order to obtain maximum power from the gas turbine, it is desirable to have a high inlet temperature combined with a high pressure ratio. Considering the maximum entry temperature permitted by turbine technology, the pressure ratio cannot be increased at will without unduly lowering the outlet temperature of the turbine and thereby severely diminishing the possibilities of steam pooduction. Even at a reasonably high turbine outlet temperature, for instance of 500-6000C, the efficiency of the heat recuperation is poor, especially when steam of high tempeature and high pressure is to he produced. When the exhaust temperature of the gas turbine is 550 C and when, by using counterflow and a minamum T of 300C between steam and exhaust gas, steam is produced in an apparatus consisting of a pre-heater, an evaporator and a superheater successively, the cooled gas will leave the plant at a temperature of 2230C if the exhaust gas is used for producing steam of 165 bar and 5200C. In a combined gas turbinesteam turbine system-based power plant built in isolation there are hardly any uses to which the excess of lcw-grade heat can be put, so that stack losses will be quite substantial and the quantity of steam produced relatively small. By accepting a lower steam pressure and/or lower temperature of superheating more heat can be recuperated from the waste gas of the gas turbine, so that the cooled gas will leave the plant at a lower temperature. Thus, if in the situation described hereinbefore the exhaust gas is used for generating steam of 80 bar and 4500C (instead of 165 bar and 5200C), the cooled gas will leave the plant at a temperature of 1870C (instead of 223 C). Although in this way more steam can be produced the amount of power that can be generated in the steam turbine will hardly grow (see Table A) owing to a loss of steam turbine efficiency. A slightly more favaurable situation presents itself when a higher gas turbine outlet temperature is utilized. When an outlet temperature of 6000C is used, the temperature of the cooled gas will be 1860C with production of 165 bar/550 C steam and 1570C with production of 80 bar/450 C steam (see Table A). Some improvement may be achieved by raising the temperature of the gas-turbine exhaust gases by combusting an additional quantity of fuel. However, this is not an ideal use of the fuel, since it generates power in the steam turbine instead of in the combined gas turbinesteam turbine system. moreover, if larger quantities of fuel are burned to obtain a maximum effect, the steam generation unit will no longer be a relatively simple unit without a combustion chamber, but it will become a more complex apparatus of the conventional type whose efficiency is relatively low due to the large excess of air required. Other measures that may be contemplated in order to improve the recuperation of low-grade heat from the exhaust gas of the gas turbine, for instance including a lcw-pressure steam cycle, are not very attractive since they increase the complexity of the plant and, in view of the temperature levels involved, have only low efficiency. TABLE A Power generation frcm gas turbine exhaust gas without additional heat supply #Tmin=30 C exhaust gas = 1.118 kJ.kg -. C steam cossessor: P = 0.04 bar, T = 290C EMI4.1 <tb> Gas <SEP> turbine <SEP> outlet <SEP> temperature, <tb> C <SEP> 550 <SEP> 600 <tb> Pressure <SEP> of <SEP> steam, <SEP> bar <SEP> 165 <SEP> 80 <SEP> 165 <SEP> 80 <tb> Temperature <SEP> of <SEP> steam, <SEP> C <SEP> 520 <SEP> 450 <SEP> 550 <SEP> 450 <tb> Steam <SEP> produced, <SEP> kg/kg <tb> exhaust <SEP> gas <SEP> 0.1134 <SEP> 0.1286 <SEP> 0.1397 <SEP> 0.1571 <tb> Heat <SEP> recupered, <SEP> kJ/kg <tb> exhaust <SEP> gas <SEP> 365.9 <SEP> 405.5 <SEP> 462.5 <SEP> 495.3 <tb> Temperature <SEP> of <SEP> stack <SEP> gas, <SEP> C <SEP> 223 <SEP> 187 <SEP> 186 <SEP> 157 <tb> Efficiency <SEP> of <SEP> steam <SEP> turbine, <SEP> % <SEP> 40.5 <SEP> 36.5 <SEP> 41 <SEP> 36.5 <tb> Effective <SEP> power, <SEP> kJ/kg <tb> exhaust <SEP> gas <SEP> 148.2 <SEP> 148.0 <SEP> 189.6 <SEP> 180.8 <tb> A much more elegant solution to the problem of the utilization of heat may be found in ccanbining the generation of power with high-temperature hydrocarbon synthesis and utilizing at least part of the high-grade waste heat of the hydrocarbon synthesis reaction evaporating water in the production of steam as the feed for the steam turbine. By combining the two processes in such a way that on the one hand unconverted synthesis gas, together with gases by-products formed, is used as fuel for the gas turbine, whilst on the other hand waste heat from the hydrocarbon synthesis is used for producing high-pressure steam the drawbacks both of the high-temperature hydrocarbon synthesis for the preparation of liquid hydrocarbons and of the combined gas turbine-steam turbine system, which present themselves when these two processes are each used in isolation, are overcome. The above-mentioned "high-temperature hydrocarbon synthesis" refers to a hydrocarbon synthesis which is carried out at a temperature above 3000C. The products of said hydrocarbon synthesis are aliphatic and/or aromatic hydtocarbcns, but not oxygenates like methanol, although oxygenates may be intermediates in the production of hydrocarbons frcm synthesis gas. The present patent application therefore relates to a process for the generation of power and the preparation of liquid hydrocarbsrs, in which of a mixture of carbon monoxide and hydrogen less than 70%v is canverted by means of a hydrocarbon synthesis carried out above 3000C, in which fran the reaction product are separated a liquid fraction which in addition to unconverted carbon monoxide and hydrogen, comprises light hydrocarbons formed during the synthesis and which latter fraction is combusted, in which the combustion gas is used for generating power in a gas turbine, in which high-pressure steam is produced from water by preheating, vaporization and superheating by using the exit gas of the gas turbine, in which the high-pressure steam is used for generating power in a steam turbine and in which at least part of the reaction heat from the hydrocarbon synthesis is used in the vaporization step of the steam production. The process proposed here is very suitable for handling both hydrogen-rich and low-hydren synthesis gases. With a proper choice of catalyst the high-terrerature hydribon conversion allows of partial conversion of lowhydrogen synthesis gases into liquid hydrocarbons without the necessity of previously subjecting the synthesis gas to the water gas shift reaction as is often required in methanol synthesis. At equal pressures (for instance 30 bar) higher conversion can be achieved in the high-temperature hydrccarbon synthesis than in the methanol synthesis. The high-temperature hydrocarbon synthesis releases more heat (20-25% of the energy content of the synthesis gas) than the methanol synthesis. Since the former reaction takes place at a high temperature, this high-grade heat can be put to good use, viz. in the vaporization step during the production of high-pressure steam which can be utilized in the steam cycle of the power plant. For instance, the reaction heat which is released when the hydrocarbon synthesis is carried out at a temperature of 375-4000C can be very well used for producing steam of 3500C and 165 bar. The high-temperature hydrocarbon synthesis may yield in addition to liquid hydrxcaxtxrs, considerable quantities of gaseous hydrocarbons (C1-C4 paraffins). However, when the high-terarature hydrocarbon synthesis is used in combination with power generation, this presents no difficulties, since these gaseous hydrocarbons fully contribute to the energy content of the fuel for the power plant and - as far as the calorific value of this fuel is concerned - even make up to sate content for the diluting effect of 002 which may be present in the fuel for instance as a result of an internal water gas shift reaction occurring during the hydrocarbon synthesis starting fran a low-hydrogen synthesis gas. So long as the gas combustible there is no objection to the presence of 002 since it can have the sate function as excess air of restricting the combustion temperature, with the advantage that the C02 is already under pressure. Since many catalysts used in the hightemperature hydrocarbens synthesis have a much higher sulphur tolerance than several rtethanol synthesis catalysts, like a Cu/ZnO catalyst, the sulphur-removing process required in the hydrocarbon synthesis when sulphur-containing synthesis gases are used - such as those formed during the gasification of coal - will be of a much simpler nature. In the high-temperature hydrocarbon synthesis it is extremely difficult to attain a synthesis gas conversion of more than 70%v when using a space velocity which is acceptable in practice, but no recirculation. However, when the high-teeperature hydrocarbon synthesis is used in combination with power generation, this presents no difficulties, since in this combination the synthesis gas is meant to be converted only partly. Depending on the catalyst chosen, the high-terprature hydrocarbon synthesis may yield either substantially aromatic hydrocarbons, or substantially paraffinic hydrocarbons. If substantially aromatic hydrocarbons are to be prepared, preference is given to the use of a bifunctional catalyst combination comprising one or more metal components having catalytic activity for the conversion of a H2/CO mixture into acyclic hydrocarbons and/or acyclic oxygen-containing organic compounds and a crystalline metal silicate of a special structure which is capable of catalysing the conversion of acyclic compounds into aromatic hydrocarbons. If substantially paraffinic hydrocarbons are to be prepared, preference is given to the use of an iron-containg catalyst having activity for the conversion of a H2/CO mixture into paraffinic hydrocarbons. As observed hereinbefore, the process according to the invention may be applied to both hydrogen-rich synthesis gases and low-hydrogen synthesis gases. The process according to the invention is of particular interest for application to load hydrogen synthesis gases. Such synthesis gases having a H2/CO nolar ratio of less than 2.0 may very suitably be obtained by gasification of carbonaceus materials, such as brown coal, anthracite, coke, crude mineral oil and fractions thereof, as well as oils produced from tar sand and bituminous shale. The gasification is preferably carried out at a temperature of 900-15000C and a pressure of 10-100 bar. In the process according to the invention the preferred starting material is a synthesis gas having a H2/CO molar ratio higher than 0.25. If in the process according to the invention the starting material is a low-hydrogen synthesis gas, the catalyst preferably used in the high-temperature hydrocarbon synthesis is a bi- or trifunctional catalyst the latter catprising, in addition to the components of a bifunctional catalyst, one or more metal components having CO-shift activity. If the high-temperature hydrocarbon synthesis is carried out with the object of preparing substantially aromatic hydrocarbons, preference is given to the use of a bi- or trifuctional catalyst which, in addition to the mental ccmponents having catalytic activity, comprises a crystalline metal silicate of a special structure which is capable of catalysing the conversion of acyclic hydrocarbons and acyclic oxygen-containing organic compounds into aromatic hydrocarbons, the metal silicate being described e.g. in British patent specification No. 1,555,928 and British patent application No. 2,055,893. If the aim of the high-temperature hydrocarbcn synthesis is to prepare substantially paraffinic hydrocarbons while starting fran a low-hydrogen synthesis gas, preference is given to the use of an iron-contaning bifunctional catalyst or catalyst combination which, in addition to activity for the conversion of a H2/OO mixture substantially into paraffinic hydrocarbons, has CO-shift activity. Preference is given to the use of a bifunctional catalyst prepared by impregnation and comprising iron supported on a carrier. Examples of such catalysts are Fe//Al2O3 and Fe/Cr/SiO2 catalysts described in British patent specification No. 2,053,713 and No. 2,053,016, respectively. Suitable conditions for carrying out the high temperature hydrocarbon synthesis are a temperature of 300-4500C, a pressure of 20-80 bar and a space velocity of 200-2000 Nl gas/l catalyst/ hour. When the high temperature hydrocarbon synthesis is used for the preparation of substantially aromatic hydrocarbons, the following conditions are preferably used: a teepature of 325-4000C, a pressure of 30-60 bar and a space velocity of 300-3000 Nl gas/l catalyst/hour. When the high-temperature hydrocarbon synthesis is used for the preparation of substantially paraffinic hydrocrabons, the following conditions are preferably used: a temperature of 300-3500C, a pressure of 20-50 bar and a space velocity of 500-2000 Nl gas/l catalyst/hour. Conversion in the high-temperature hydrocarbon synthesis should be less than 70%v. Depending on the object pursued the conversion may vary within wide limits. Usually the conversion will be more than 10%v. In general, the process according to the invention can be used for the generation of power and the preparation of liquid hyaaocarbs from matures of carbon monoxide and hydrogen. The process is of particular interest for the generation of electricity and the preparation of synthetic gasoline, starting fran low-hydrogen synthesis gas obtained in the high-pressure gasification of coal. Excellent catalysts for the conversion of low-hydrogen synthesis gases into synthetic gasolines are the afore-mentioned tri functional catalyst combinations consisting of a mixture of catalyst capable of converting a H2/CO mixture substantially into methanol and a crystalline metal silicate of a special structure capable of converting methanol into aromatic hydrocarbons. Since the use of these catalysts results in a liquid product which boils substantially in the gasoline range, this hydrocarbon synthesis is sometimes referred to as the "direct gasoline synthesis" (DGS). Hereinafter whenever mention is made of DGS, it will be to designate the direct gasoline synthesis described hereinbefore. In power plants periods of normal load and periods of peak load succeed each other. In order to be able to meet the demand for power in peak load periods, supplementary fuel is supplied to the gas turbine. To this end the process according to the invention utilizes the liquid hydrocarbons prepared by way of the high-tettprature hydrocarbon synthesis. Depending on the quality of the liquid hydrocarbons produced by higb-tetrlperatuue hydrocarbon synthesis, it may in sate cases be more attractive to purchase the supplementary fuel needed to cope with peak loads elsewhere and to reserve the liquid hydrocarbons prepared in the process for other purposes. Such a situation may present itself, for instance, when the hydrocarbon synthesis is carried out as a DGS, which yields an extremely valuable product that can be put to excellent use as motor gasoline. However, as may be seen fran the following, the process according to the invention is highly flexible, so that to a certain extent it is possible to meet fluctuations in power demand without having to fall back on supplementary fuel purchased from external sources or produced in situ. The DGS produces a considerable quantity of reaction heat of a temperature level of 375-4000C. A reactor that is very suitable for carrying out the DGS is a reactor whose heat discharge takes place by means of internal cooling pipes in which the heat is absorbed by water which boils, for instance, at 3500C and 165 bar. If the synthesis reactor is situated on the same site as the power plant, this provides an excellent opportunity for integrating this steam system into the combined gas turbine-steam turbine system. Preferably, the DGS is carried out isothermally, so that it releases the heat at a very attractive constant temperature level. Therefore this heat is excellently suitable for providing the heat of vaporization during the production of high-pressure steam and the utilization of the heat present in the exhaust gas of the gas turbine can be principally restricted to heating the water and spperheating the steam. Data of situations in which 50 and 100%, respectively, of the heat of vaporization is provided by the DGS show that the process may be carried out more efficiently. (See Tables B and C). In particular in the case where 100% of the heat of vaporization is provided by the DGS the countercurrent exchange of heat is virtually ideal, resulting in a maximum gain of heat .fran the exhaust gas and consequently very low stack temperatures, of 91 and 670C at gas turbine outlet temperatures of 550 and 6000C, respectively. The almost maximum quantity of heat recovered fran the exhaust gas and the heat produced by the synthesis reaction together became available as high-pressure superheated steam (165 bar, 520-5500C) which can be converted into power with good efficiency. Not only is in this way the reaction heat of the hydrocarbon synthesis - which usually becomes available as saturated steam - upgraded, but more steam is produced besides. As shown in Table C, the reaction heat of the DGS is transformed to an additional quantity of superheated high pressure steam with an apparent efficiency of about 170% and finally it is transformed to extra power with an energy efficiency of about 70%. This is almost three times as high as when the reaction heat would have been simply utilized for the production of saturated steam to be used for the generation of power in a separate steam cycle of relatively poor efficiency. Not only is the latter option inferior fran an energetic point of view, it is more costly as well, since a separate steam cycle has to be added to the system. TABLE B Power generation fran gas turbine exhaust gas, in which the reaction heat of a DGS supPlies at least part of the heat of vaporization of the water =30 C exhaust gas = 1.118 kJ.kg P steam condensor: P = 0.04 bar, T = 29 C EMI12.1 <tb> Gas <SEP> turbine <SEP> outlet <SEP> temperature, <SEP> <tb> C <SEP> 550 <SEP> 600 <tb> Pressure <SEP> of <SEP> steam, <SEP> bar <SEP> 165 <SEP> 165 <tb> Temperature <SEP> of <SEP> steam, <SEP> C <SEP> 520 <SEP> 550 <tb> % <SEP> of <SEP> heat <SEP> of <SEP> vaporization <tb> supplied <SEP> by <SEP> DGS <SEP> 50 <SEP> 100 <SEP> 50 <SEP> 100 <tb> Steam <SEP> produced, <SEP> kg/kg <tb> exhaust <SEP> gas <SEP> 0.151 <SEP> 0.220 <SEP> 0.182 <SEP> 0.247 <tb> Heat <SEP> recovered, <SEP> kJ/kg <tb> exhaust <SEP> gas <SEP> 419.6 <SEP> 512.9 <SEP> 521.1 <SEP> 596.5 <tb> Temperature <SEP> of <SEP> stack <SEP> gas, <SEP> C <SEP> 170 <SEP> 91 <SEP> 134 <SEP> 67 <tb> Heat <SEP> supplied <SEP> by <SEP> DGS, <SEP> kJ/kg <SEP> <tb> exhaust <SEP> gas <SEP> 67.6 <SEP> 197.0 <SEP> 81.5 <SEP> 221.3 <tb> Total <SEP> steam <SEP> energy, <SEP> kJ/kg <tb> exhaust <SEP> gas <SEP> 487.3 <SEP> 709.9 <SEP> 602.6 <SEP> 817.8 <tb> Steam <SEP> turbine <SEP> efficiency, <SEP> % <SEP> 40.5 <SEP> 40.5 <SEP> 41 <SEP> 41 <tb> Effective <SEP> power, <SEP> kJ/kg <SEP> <tb> exhaust <SEP> gas <SEP> <SEP> 197.4 <SEP> 287.5 <SEP> 247.1 <SEP> 335.3 <SEP> <tb> TABLE C Effect of integration of DGS into a combined gas turbine-steam turbine system on power generation in steam cycle EMI13.1 <tb> <SEP> Gas <SEP> turbine <SEP> <SEP> outlet <SEP> Gas <SEP> turbine <SEP> <SEP> outlet <tb> <SEP> temperature <SEP> 5500C <SEP> temperature <SEP> 6000C <tb> <SEP> Psteam <SEP> = <SEP> 165 <SEP> bar <SEP> Psteam <SEP> = <SEP> 165 <SEP> bar <tb> <SEP> steam <SEP> = <SEP> <SEP> steam <SEP> <SEP> T <SEP> 5500C <SEP> <tb> % <SEP> of <SEP> heat <SEP> of <SEP> vaporization <tb> supplied <SEP> by <SEP> DGS <SEP> 0 <SEP> 50 <SEP> 100 <SEP> 0 <SEP> 50 <SEP> 100 <tb> Temperature <SEP> of <SEP> stack <SEP> gas, <tb> <SEP> C <tb> Steam <SEP> produced, <SEP> kg/kg <tb> exhaust <SEP> gas <SEP> 0.113 <SEP> <SEP> 0.151 <SEP> 0.220 <SEP> 0.140 <SEP> 0.182 <SEP> 0.247 <tb> Total <SEP> steam <SEP> energy, <SEP> kJ/kg <tb> exhaust <SEP> gas <SEP> 365.9 <SEP> 487.3 <SEP> 709.9 <SEP> 462.5 <SEP> 602.5 <SEP> 817.8 <tb> Extra <SEP> steam <SEP> energy <tb> produced <SEP> = <SEP> #S, <SEP> <SEP> kJ/kg <tb> exhaust <SEP> gas <SEP> 0 <SEP> 121.4 <SEP> 341.0 <SEP> 0 <SEP> 140.1 <SEP> 355.3 <tb> <SEP> Heat <SEP> supplied <SEP> by <SEP> DGS <SEP> = <tb> #, <SEP> <SEP> kJ/kg <SEP> exhaust <SEP> gas <SEP> 0 <SEP> 67.6 <SEP> 197.0 <SEP> 0 <SEP> 81.5 <SEP> 221.3 <tb> TABLE C (cont'd) EMI14.1 <tb> <SEP> Gas <SEP> turbine <SEP> outlet <SEP> Gas <SEP> turbine <SEP> outlet <tb> <SEP> temperature <SEP> 5500C <SEP> temçerature <SEP> 6000C <tb> <SEP> Psteam <SEP> = <SEP> 165 <SEP> bar <SEP> Psteam <SEP> = <SEP> 165 <SEP> bar <tb> <SEP> Steam <SEP> = <SEP> 5200C <SEP> T <SEP> = <SEP> 5500C <tb> Apparent <SEP> efficiency <SEP> of <tb> utilization <SEP> of <SEP> DGS <SEP> reac <tb> tian <SEP> heat <SEP> = <SEP> #S/#, <SEP> <SEP> % <SEP> - <SEP> 179 <SEP> 175 <SEP> - <SEP> 172 <SEP> 169 <tb> Extra <SEP> power <SEP> generated <SEP> = <tb> DE, <SEP> kJ/kg <SEP> exhaust <SEP> gas <SEP> 0 <SEP> 49.2 <SEP> 139.2 <SEP> 0 <SEP> 57.5 <SEP> 152.0 <tb> Efficiency <SEP> of <SEP> conversion <tb> DGS <SEP> reaction <SEP> heat <SEP> into <tb> power <SEP> = <SEP> #E/# <SEP> <SEP> % <SEP> - <SEP> 73 <SEP> 71 <SEP> - <SEP> 71 <SEP> 69 <tb> As already observed hereinbefore, the process according to the invention has a high degree of flexibility, so that, within certain limits, it is possible to meet fluctuations in power demand. for in the process according to the invention an increase in demand for power can be excellently met by reduction of the conversion in the hydrocarbon synthesis, resulting in more synthesis gas becoming available for use as fuel gas for the generation of power. The necessary fluctuations in degree of conversion in the hydrocarbon synthesis are preferably achieved by feeding part of the synthesis gas into the gas turbine by way of a by-pass around the synthesis reactor. According as more synthesis gas is diverted, the space velocity in the reactor will decrease. This reduces the absolute quantity of synthesis gas converted and, consequently the conversion based on the total quantity of synthesis gas feed. Since the reactor tempera ture is largely controlled by the boiling water in the internal cooling pipes, a reduction in the gas flow rate will have but little effect on the reactor temperature. The invention is now elucidated with the aid of the following example. EXAMPLE In order to assess the advantages of the integration of a DGS into a combined gas turbine-steam turbine system (CGSS), four schemes were elaborated describing the conversion of coal into nothing but electricity (A), into nothing but gasoline (D) and intq both gasoline and electricity (B and C). In scheme B the same amount of electricity was generated as in scheme A, while the relative ratio between gasoline, energy and electricity were such that the reaction heat of the DGS supplied 100% of the heat of vaporization, whereas in scheme C only half this quantity of heat was supplied. The Table D was made with the aid of the following data: Coal feed : Ash content 12%w; moisture content 6.5%w; Analysis of coal: 78.1%w C; 5.5%w H; 4.3%w S; 1.2%w N; lO.9%w 0. Calorific value 31.6 MJ/kg noisture and ash free coal (MF coal). Gasification : High-pressure gasification using a mixture of steam and oxygen. Temperature 15000C; pressure 30 bar; residence time of coal in reactor: 0.55 s. O2/MF coal = 0.89 kg/kg H20/MAF coal = 0.08 kg/kg Yield: 1.99 Nm3 purified synthesis gas per kg MF coal having the composition: 32.8%v H2; 66.5 %v CO; 0.7%v N2 + Ar. Calorific value of synthesis gas: 12 MJ/Nm . Energy needed for preparing oxygen and process steam is supplied by a waste heat boiler integrated into the coal gasifier. Hydrocarbon : DGS over a catalyst consisting of a mixture of a synthesis ZnO-Cr2O3 composition and a crystalline iron/ aluminium silicate of a special structure, as disclosed in British patent specification No. 1,555,928 P = 30 bar, T = 4000C. C3+ selectivity: 95%w on C1+. C5+ selectivity: 80%w on C1+. Gas turbine : Efficiency expressed as specific energy consumption: 11290 kJ/kWh Inlet temperature: 11300C Outlet temperature: 5520C Pressure ratio + 14.2:1 Air flow rate 12.35 t/MWh Exhaust gas : preheater + spperheater boiler iST = 300C, minimally Steam turbine: Psteam = 165 bar; Tsteam = 520 C Pcondensor = 0.04 bar; Tcondensor = 29 C Energy conversion efficiency: 40.5% In Table D the most significant results of the schemes are given. In scheme B about 35% more coal is gasified than in scheme A and about half of the synthesis gas is converted into gasoline. Although as compared with scheme A, less CO and H2 is left over for use as fuel for the gas turbine, the same amount of electric power is produced. In case of gasoline production of approxImately the same energy content the total effective energy produced by scheme B is almost redoubled. The thermal efficiency of the coal conversion has been increased fran less than 40% to over 50%. Comparison of scheme B with scheme D and scheme A shows that a quantity of 173 t/h of coal would be needed to produce about the sate quantities of electricity and gasoline as produced in scheme B starting from 134 t/h. This clearly shows the advantage to be obtained fran the integration of the two processes. As regards peak shaving, the following may be observed. If the integrated process is constructed in such a way that scheme B (about 50% synthesis gas conversion in DGS) corresponds with the base load, an increase in electricity demand can be met within certain limits by reduction of the conversion, so that more gas is available for use as fuel for the CGSS. In scheme C the same quantity of coal (134.5 t/h) is supplied to the gasifier as in scheme B, but conversion in the DGS is reduced to 24%. Consequently the quantity of electricity produced grows (from 323 to 375 MW). As is seen from Table D, virtually the entire increase in electric power occurs in the section of the CGSS which is connected with the gas turbine, whereas the section connected with the steam production is barely involved. This is very fortunate, since rapid response and relatively low.cost itiake gas turbines eminently suitable for peak shaving. Thus, by installing sufficient gas turbine capacity, fluctuations in the demand for electricity can be met to a certain extent, while the most important and itost costly parts used in the ccversicn of coal to electricity are constantly operated at full capacity. The advantages of integration are still quite substantial at a low degree of synthesis gas conversion. TABLE D EMI18.1 Scheme <SEP> A <SEP> B <SEP> C <SEP> D <tb> <SEP> only <SEP> Gasoline <SEP> and <SEP> Gasoline <SEP> and <SEP> Only <tb> <SEP> electricity <SEP> electricity, <SEP> electricity, <SEP> gasoline <tb> <SEP> 100% <SEP> of <SEP> heat <SEP> 50% <SEP> of <SEP> heat <tb> <SEP> of <SEP> vaporisation <SEP> of <SEP> vaporisation <tb> <SEP> of <SEP> water <SEP> of <SEP> water <tb> <SEP> supplied <SEP> by <SEP> DGS <SEP> supplied <SEP> by <SEP> DGS <tb> Coal <SEP> supply, <SEP> t/h <SEP> MAF <SEP> 100.0 <SEP> 134.5 <SEP> 134.5 <SEP> 73.4 <tb> MW <SEP> equivalent <SEP> 878 <SEP> 1180 <SEP> 1180 <SEP> 644 <tb> Synthesis <SEP> gas <SEP> produced, <tb> 10 <SEP> Nm /h <SEP> 199 <SEP> 268 <SEP> 268 <SEP> 146 <tb> MW <SEP> equivalent <SEP> 663 <SEP> 8920 <SEP> 8920 <SEP> 487 <tb> Synthesis <SEP> gas <SEP> converted <tb> in <SEP> synthesis <SEP> step, <SEP> % <SEP> -- <SEP> 51.8 <SEP> 24.0 <SEP> 95.0 <tb> C5+ <SEP> gasoline <SEP> produced, <tb> t/h <SEP> -- <SEP> 23.1 <SEP> 11.2 <SEP> 23.1 <tb> MW <SEP> equivalent <SEP> -- <SEP> 276 <SEP> 134 <SEP> 276 <tb> TABLE D (cont'd) EMI19.1 Scheme <SEP> A <SEP> B <SEP> C <SEP> D <tb> <SEP> only <SEP> Gasoline <SEP> and <SEP> Gasoline <SEP> and <SEP> Only <tb> <SEP> electricity <SEP> electricity, <SEP> electricity, <SEP> gasoline <tb> <SEP> 100% <SEP> of <SEP> heat <SEP> 50% <SEP> of <SEP> heat <tb> <SEP> of <SEP> vaporisation <SEP> of <SEP> vaporisation <tb> <SEP> of <SEP> water <SEP> of <SEP> water <tb> <SEP> supplied <SEP> by <SEP> DGS <SEP> supplied <SEP> by <SEP> DGS <tb> Electricity <SEP> generated, <SEP> MW <tb> Gas <SEP> turbine <SEP> 212 <SEP> 160 <SEP> 221 <SEP> - Steam <SEP> turbine <SEP> 111 <SEP> + <SEP> 163 <SEP> + <SEP> 154 <SEP> + <SEP> - Total <SEP> 323 <SEP> 323 <SEP> 375 <SEP> - Total <SEP> useful <SEP> energy <tb> produced, <SEP> MW <SEP> 323 <SEP> 599 <SEP> 509 <SEP> 276 <tb> Thermal <SEP> efficiency <tb> (synthesis <SEP> gas <SEP> to <tb> useful <SEP> products), <SEP> 48.7 <SEP> 67.2 <SEP> 57.1 <SEP> 56.9 <tb> Thermal <SEP> efficincy <tb> (coal <SEP> to <SEP> useful <SEP> products), <tb> % <SEP> 36.9 <SEP> 50.8 <SEP> 43.1 <SEP> 42.9 <tb>

Claims: CLAIMS 1. A process for the generation of power and the preparation of liquid hydrocarbons, characterized in that of a mixture of carbon monoxide and hydrogen less than 70Pv is converted by means of a hydrocarbon synthesis carried out above 3000C, that from the reaction product are separated a liquid fraction which ccmprises the desired hydrxcarbsrs and a gaseous fraction which, in addition to unconverted carbon monoxide and hydrogen, comprises light hydrocarbcns formed during the synthesis and which latter fraction is combusted, that the combustion gas is used for generating power in a gas turbine, that high pressure steam is produced fram water by pre-heating, vaporization and superheating by using the hot exit gas of the gas turbine, that the high-pressure steam is used for generating power in a steam turbine and that at least part of the reaction heat from the hydrocarbon synthesis is used in the vaporization stage of the steam production. 2. A process as claimed in claim 1, characterized in that the hydrocarban synthesis is carried out at a temperature of 300-4500C, a pressure of 20-80 bar and a space velocity of 200-2000 N1 gas/l catalyst/hour. 3. A process as claimed in claim 1 or 2, characterized in that it is applied to a synthesis gas having a H2/CO molar ratio in the range between 0.25 and 2.0. 4. A process as claimed in claim 3, characterized in that it is applied to a synthesis gas obtained in the gasification of coal at a temperature of 900-15000C and a pressure of 10-100 bar. 5. A process as claimed in any one of claims 1-4, characterized in that it is used for the generation of electricity and for the preparation of gasoline. 6. A process as claimed in any one of claims 1-5, characterized in that all the heat required for the vaporization of water in the steam production is supplied by the hydrocarbon synthesis. 7. A process as claimed in any one of claims 1-6, characterized in that an increase in demand for power is met by reduction of the conversion in the hydrccartcn synthesis, resulting in more synthesis gas becaning available for use as fuel gas for the generation of power. 8. A process as claimed in claim 7, characterized in that reduction of the conversion in the hydrocarbon synthesis is achieved by feeding part of the synthesis gas into the gas turbine by way of a by-pass around the synthesis reactor. 9. A process for the generation of power and the preparation of liquid hydrocarbons as claimed in claim 1, substantially as described hereinbefore and in particular with reference to the example. 10. Power whenever generated and liquid hydrocarbons whenever prepared according to a process as described in claim 9.

Inventors: SIE, SWAN TIONG
Applicants: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.
Application year: 1983
Main classification: F01K23
IPC codes: C07C1, F01K23, C10G2, C07C67