PROCESS FOR THE PREPARATION OF HYDROCARBONS AND A FUEL GAS

Abstract: Process for the preparation of hydrocarbons and a fuel gas from a heavy carbonaceous feedstock, which process comprises: a) cracking the heavy carbonaceous feedstock in a coking zone which contains a bed of fluidized solids, producing hydrocarbons and coke which deposits upon the fluidized solids; b) introducing a part of the coke-containing solids into a gasification zone in which at least a part of the coke is gasified with an oxygen-containing gas yielding a carbon monoxide- and hydrogen-containing gas mixture; c) partially converting the carbon monoxide- and hyd­ rogen-containing gas mixture into hydrocarbons in a synth­ esis zone; d) separating a fuel gas comprising carbon monoxide, hydrogen and gaseous hydrocarbons, and at least one liquid hydrocarbon fraction from the product of the synthesis zone.

Description: PROCESS FOR THE PREPARATION OF HYDROCARBONS AND A FUEL GXS The present invention relates to a process for the preparation of hydrocarbons and a fuel gas fran a heavy carbonaceous feedstock, which process comprises: a) cracking the heavy carbonaceous feedstock in a coking zone which contains a bed of fluidized solids, producing hydro carbons and coke which deposits upon the fluidized solids; b) introducing a part of the coke-contahing solids into a gasitication zone in which at least a part of the coke is gasified with an oxygen-containing gas, yielding a carbon monoxide- and hydrogen-containing gas mixture; c) partially converting the carbon nonoxide- and hydrogen-con- taining gas mixture into hydrocarbons in a synthesis zone; d) separating a tuel gas comprising carbon monoxide, hydrogen and gaseous hydrocarbs, and at least one liquid hydrocarbon fraction fran the product of the synthesis zone. In the coking zone a carbaceous feedstock is cracked in a fluid bed operation. Many kinds of feedstocks may be applied, like heavy hydrocarbon oils such as long or short residues, pitch, asphalt, bitumen, tar, shale oil, coal liquetaction products, but also solid fuels like coal or slurries of coal in oil and/or water. In the coking zone hydoncarbons evaporate and remaining coke deposits upon the fluidized solids. The solids may be any solids which can resist the process conditions, like sand, silica or alumina particles. Preferably the solids are coke particles. Their size suitably is 40-1000 microns. This way no inerts are to be handled in the present process. The particles are fluidized by neans of a fluidizing gas which enters the coking zone near or through the bottom. The e fluidizing gas, preferably, is steam. The feedstock which is preferably preheated to a temperature of 250 400 OC, may be introduced into the fluidized bed through one or more nozzles. The process is suitably a thermal cracking process carried out at a temperature between 425 and 700 OC and a pressure between 1 and 15 bar. The heat to maintain the coking temperature is provided by hot solids, advantageously having a temperature of 50-150 OC above the coking temperature, which are recycled fran the gasification zone or fran a heating zone to be discussed hereafter. The steam preferably used as fluidizing gas may be preheated too, so that it adds heat to the coking zone or does not take up too much heat fran it. Suitably the fluidizing gas, such as steam, has a temperature ranging fran 400 to 600 OC, In the coking zone the feedstock yields hydrocarbons with various chain lengths. The hydrocrbus produced are preferably split up in at least one gaseous fraction and at least one liquid fraction. One may split the product of the coking zone into a gaseous fraction containing methane, ethane and ethylene, and another gaseous fraction comprising the C3 and C4 hydrocarbons. The latter fraction may be used as liquified petroleum gas (L9G). The products containing 5 or more carbon atcms per molecule, which products suitably are recovered as the liquid hydrocarbon fraction(s), may be split up into a gasoline, a kerosene, a gas oil and a residual fraction. The coke-containing solids which may consist of coke alone, are preferably continuously discharged fran the coking zone, while make up solids are fed into said coking zone. The solids discharged fran the coking zone are suitably at a temperature of 425 to 700 OC. Before being introduced into the gasification zone the coke-containing solids obtained fram the coking zone are preferably heated. Thereto any conventional heating method may be used. Very suitably, the solids are heated in a fluidized bed by means of a hot fluidizing gas and/or hot fluidized solids which act as heat carriers. Advantageously the carbon monoxide- and hydrogen-contdining gas mixture obtained in the gasification zone is applied as the hot fluidizing gas, and solids from which the coke at least partially has been converted in the gasification zone are applied as the hot fluidized solids. The coke-containing solids are preferably heated this way to a temperature between 50 and 150 OC above the temperature in the coking zone at a pressure between 1 and 15 bar. After the preferred heating the coke-containing solids are introduced into the gasification zone. The solids fram which part of the coke has been converted, may then be applied as heat carrier in the heating and/or the coking zone. Preferably, the gasification is carried out in a fluidized bed. In the fluidized bed the temperature is regulated such that no melting of the solids occurs. Very suitably the oxygen-containing gas acts as fluidizing gas. The oxygen-containing gas may be air, oxygen-enriched air or oxygen. The oxygen-containing gas may be mixed with steam. Preferably the oxygen-containg gas is air, since this way the costs of an expensive air separation plant are saved. Steam which is preferably introduced into the gasification zone, may be passed thereto together with and/or apart from the oxygen-containing gas. As to the quantities of steam and oxygen-containing gas being introduced into the gasification zone, they are regulated such that the gasification is carried out at a temperature of 800 to 1200 OC and a pressure between 1 and 15 bar. When the solids consist of coke alone, the amounts of air and steam are such, that only a portion of the coke is gasified so that hot coke particles remain. The portion of coke gasified preferably corresponds with 90 % or more of the net coke production in the coking zone. In case of inert solids upon which coke is deposited, the amounts of air and steam are advantageously such that over 90 % of the coke is converted, yielding hot inert solids. Very suitably at least a part of the hot solids fran which coke has been gasified, are recycled to the coking zone as heat carrier. When there is a heating zone between the coking and the gasification zones the hot solids from the gasification zone are preferably passed to the heating zone and subsequently fran the heating zone to the coking zone. Ash which may be formed, is discharged tran the gasification reactor. When the above integrated process of coking and gasification is carried out at a commercial scale, a great quantity of coke is formed and a vast amount of carbon monoxide- and hydrogen-contain- mg gas is produced. The heating value of the latter gas is relatively low since it contains in addition to carbon monoxide and hydrogen and hydrogen sulphide, a relatively high percentage of non coEtustibles such as carbon dioxide, steam, and nitrogen. Advantageously, the gas is desuiphurized and Then used as fuel gas in a furnace or a similar apparatus on the refinery in which the integrated process has been incorporated. Operation on commercial scale, however, involves a too great production of this low heating value gas so that not all the gas produced can be usefully combusted in furnaces close to the process plant. Moreover, transport of a part of this gas over longer distances usually involves too high expenses. According to the invention the gas is partially converted mto hydzocastoos. By means of the partial conversion a such stantial amount of hydrocarbons are produced. The hydrocarbons include normally gaseous and normally liquid hydrobons. The normally liquid hydrocarbons are very useful as fuel or chemical teedstock. The normally gaseous hydrocarbons are discharged fran the synthesis zone with the off-gas which contains in addition to the normally gaseous hydrocarbons and some carbon monoxide and hydrogen, nitrogen. The high heating value of the normally gaseous hydrocarbons warrant a sufficient heating value of the off-gas. The volume of the off-gas is of course substantially smaller than the volume of the carbon monoxide- and hydrogen-containing gas subjected to the conversion. For this conversion the carbon monoxide- and hydrogen-con- taining gas mixture is contacted with a catalyst. Since most heavy carbonaceous feedstocks contain sulphur, the carbon monoxide- and hydrogen-containing gas mixture produced in the gasification zone usually contains some hydrogen sulphide. It is desirable to remove at least most of the hydrogen sulphide as practically all catalysts which are applicable in the conversion are more or less severely poisoned by sulphur compounds. Moreover, in order to avoid environmental pollution fuel gases are advantageously sulphur-free. Therefore, the gas mixture from which fuel gas is produced according to the invention is preferably desulphurized. To desulphurize the gas mixture any conventional desulphurization process may be used. Very suitable are processes in which hydrogen sulphide and optionally part of the carbon dioxide present in the gas mixture are absorbed by an absorbing liquid. Very suitable are the ADIP - and Sulfinol processes, described in British patent specification Nos. 1,131,989, 972,140, 965,358, 957,260 and 879,090. The purified remaining gas is preferably contacted with a Fischertapsch catalyst for the production of hydrocarbons from hydrogen and carbon monoxide. Most Fisccer-Trcpsch catalysts yield hydrocarbcns in the range from 1 to over 30 carbon atams per molecule. Especially the preparation of methane or a C1-C4 hydrocarbon mixture is disadvantageous since in the coking zone considerable amounts of methane and other light hydrocarbons (cm ) have already been obtained. So an overproduction of these cheap gases should be avoided. Very suitably the conversion is carried out such that a substantial amount of liquid hydrocarbons is prepared. So, preferably a Fischer-Tropsch catalyst is selected, which catalyst is capable of catalysing the conversion of a hydro gen/carbon monoxide gas mixture into liquid hydrocarbons. The catalyst preferably is able to stand considerable amounts of nitrogen and/or carbon dioxide in the hydrogen- and carbon mono xide-containing gas mixture. In said gas mixture 20 to 60 % vol of nitrogen and 0 to 10 % vol of carbon dioxide may be present. Therefore, m the synthesis zone the carbon monoxide- and hydrogen-containing gas mixture is contacted preferably with a catalyst comprising cobalt and at least one metal selected from ruthenium, zirconium, titanium and chromium on silica, silica-alumina or alumina as carrier. These catalysts are found to be stabilized in the presence of nitrogen and/or carbon dioxide. Moreover, they are excellent catalysts for the conversion of carbon monoxide- and hydrogen-containing gas °mixtures into hydrocarbons boiling in or above the kerosene and gas oil range. They are applicable at pressures within a wide range. They are preferably used at pressures tran 5 to 50 bar. The catalyst preferably comprises 3-60 pbw of cobalt and 0.1 - 100 pbw of ruthenium, zirconium, titanium and/or chromium per 100 pbw of carrier. The catalyst suitably has been prepared by impregnation of the carrier with a solution of one or more ccupoonds of the metal or mentals. This includes both a simultaneous impregnation of the carrier by a solution containing all metals involved, and a subsequent deposition of each metal separately by jirpregnation. It is also very suitable to use a catalyst prepared by kneading the carrier with one or more compounds of the metal or metals in the presence of a liquid. The methods of preparation are well described in British patent specification No. 2,077,289 and Netherlands patent application Nos. 8204525 and 8203066. The dependence of the catalyst performance on the cobalt load and the surface area of the catalyst is described in Netherlands patent application No. 8301922. The most preferred catalyst comprises 15-50 pbw of cobalt and 0.1-40 pbw of zirconium on 100 pbw of silica. The process conditions under which the conversion in the synthesis zone is carried cut are preferably a temperature between 175 and 300 OC, a pressure between 5 and 50 bar and a space velocity from 200 to 2000 N1. l.hr 1. The conversion is a strongly exothermic reaction. Therefore the reaction heat is preferably recovered in the form of steam. This steam may be used as fluidizing gas in the coking zone. The degree of the conversion in the synthesis zone is determined depending on the quantity of low heating value gas required in the refinery plant. So, advantageously the carbon monoxide- and hydrogen-containing gas mixture is converted for 30 to 70 % vol, calculated on the volume of carbon monoxide and hydrogen. Due to the fact that the gas mixture is converted partially the off-gas of the conversion still contains some carbon monoxide and hydrogen. Even when a catalyst is used which is capable of catalysing the conversion of carbon monoxide and hydrogen into liquid hydrocarbs same gaseous hydrtcarbcrs are inevitably formed. The latter hydrocarbons are discharged with the off-gas together with the unconverted gases and steam formed during the conversion. One should expect that the decreased amount of carbon monoxide and hydrogen in the ott-gas, would involve a proportional decrease of the heating value of the off-gas. The high heating value of the gaseous hydrocarbons and the decreased volume however warrants that the off-gas as a whole has a heating value cam- parable to or not much lower than that of the carbon monoxide- and hydrogen-containing gas mixture used in the conversion. Further a considerable quantity of liquid hydrocarbons is produced. So, by the above partial conversion a reduction in the quantity of the low heating value gas is achieved while the quality of the remaining low heating value gas is still at a sufficient level, and valuable liquid hydrocarbons are obtained in a considerable quantity. The heating value of the fuel gas obtained suitably is between 3 and 10 MJ/Nm3. It may be advisable to upgrade the heating value of the otf-gas of the synthesis zone when its heat value is rather low, e.g. when the carbon monoxide and hydro gen-containing gas mixture has been converted almost exclusively into normally liquid hydroarbons. For this purpose, the fuel gas obtained after separation from the product of the synthesis zone is preferably blended with at least a part of the gaseous hydrocarbons- containing fraction obtained from the product of the coking zone. So, for mstance a part of the methane and C2 hydrocarnons produced in the coking zone are added to the fuel gas, the heating value of the gas so obtained being increased thereby. The liquid hydkccarbon fractions obtained after separation fran the product of the synthesis zone are of excellent quality, especially the kerosene and gas oil fractions are excellent. The kerosene fraction comprises especially unbranched hydrocarbon molecules which involves a high smoke point. As the gas oil fraction, too, comprises especially paraffinic hydrocarbons, it possesses a high cetane number. Therefore at least a part of a liquid hydoocarbon fraction obtained after separation from the product of the synthesis zone is preferably blended with at least a part of a liquid hydrocarbon fraction obtained from the product of the coking zone, thereby upgrading the resulting liquid fraction. The fraction boiling above the gasoil range, can be converted to lighter hydrocarbons by catalytic cracking or by hydrocracking. These lighter hydrocarbons may also be blended with appropriate fractions of the coker product. The invention will now be further illustrated with reference to the figure showing a flow scheme for the process according to the invention, in which figure auxiliary equipment, such as pumps compressors, valves, control devices, is not included. However, the invention is by no means limited to this figure. A carbonaceous feedstock is fed through a line 2 into a coking reactor 1. Inside the reactor a bed of fluidized solids, e.g. coke particles, is present, which solids are fluidized by means of steam introduced through a line 3. The hydrocarbon products and non-converted steam leave the reactor through a line 4 and are passed to a separator 5 in which the coking product is split up into a gaseous fraction discharged by a line 6, and a liquid fraction discharged by a line 7. In the reactor 1 fresh coke from the carbonaceous feedstock deposits upon the solids. Coke-containing solids are discharged at the bottom of the reactor through a line 8. They are conveyed to a heater 11 through a line 9 by means of a carrier gas comprising a hot carbon monoxide- and hydrogen-containing gas supplied through a line 10. In the heater 11 a fluidized bed of solids is present. Hot solids are introduced as heat carriers into the heater 11 through a line 14 from a gasification reactor 15. Heated solids are passed from the heater 11 to the coking reactor 1 through a line 13 and from the heater 11 to the gasification reactor 15 through a line 16. The carrier gas from lines 10 and 9 acts as fluidizing gas in the heater 11 and is discharged through a line 12. In the gasification reactor 15 coke on the solids is partially combusted by means of an oxygen-containg gas such as air and steam, supplied through a line 17, yielding hot solids, a carbon monoxide- and hydrogen-containing gas mixture and ash. The oxygen-contaning gas and steam act as fluidizing gas in the gasification reactor 15. The hot carbon monoxide- and hydrogen-containing gas is discharged through the line 10 and passed to the lines 8 and 9. Hot solids are passed to the heater 11 through the line 14 and ash is discharged from the system through a line 18. The carbon monGxide- and hydrogen-containing gas mixture is passed through the line 12 to a scrubber 19 in which hydrogen sulphide, and optionally C02 present in the gas, are removed fran the gas. The resulting gas is passed through a line 20 into a synthesis reactor 21, loaded with a bed of cobalt and zirconium-containing silica. The gas mixture is partially converted into hydrocarbons. The product of the synthesis reactor 21 is passed through a line 22 to a separator 23 in which the product is split in a fuel gas, discharged through a line 24 and a liquid fraction discharged through a line 25. The heating value of the fuel gas in line 24 may be upgraded by blending it with a part of the gaseous product of line 6. Thereto, a part of the latter product is passed fram line 6 to line 24 through a line 26. The upgraded fuel gas is discharged through a line 28. The remaInIng part of the gaseous product of the coking zone is passed for further processing through a line 27. EXAMPLE In a process as described in the figure 312 t/hr of a short residue of an Arabian heavy crude oil are passed into a coking reactor in which coke particles are fluidized with steam as a fluidizing gas and in which a te°perature of 525 0C and a pressure of 2 bar prevailes. The residue has the following properties: Density kg/m3 1050 Sulphur %w 6.0 Nitrogen %w 0.48 Conradson Carbon %w 28 Nickel ppmw 50 Vanadium ppmw 219 The rate of residue supply is equivalent to an energy rate of 3390 MW. The cracking of the residue yields 42.1 t/hr C1-C4 hydrocarbons and 161.3 t/hr liquid C5+ hydrocarbons boiling below 530 OC. Upon the coke particles present in the coking reactor, 109 t/hr of coke are deposited. A stream of coke-containing particles in excess of this amount is discharged frcan the coking reactor at a temperature of 525 OC, heated to 620 C in a heater and passed to a gasification reactor, together with a circulating stream of coke particles. In the gasification reactor 103 t/hr of coke are converted with air and steam into a carbon monoxide- and hydrogen-containing gas. This gas and a circulating stream of hot coke are passed to the heater where they are cooled by the stream of coke particles frcm the coking zone. The heat released by the hot gas and coke stream fran the gasification zone is partly passed to the coking reactor by another stream of coke particles circulating between the heater and the reactor to provide the neat required for the coking reaction. After condensation of water and removal of acidic components (19.9 t/hr H2S and 8.5 t/hr CO2) the carbon monoxide- and hydrogen-containing gas is obtained in a quantity of 460.103 Nm3/hr and has the following catposition: CO 24.3 % vol H2 21.3 N2 51.8 Other 2.6 " The heating value of the gas is 5.7 MJ/Nm . The gas production represents 730 MW, i.e. 21.6 % of the energy introduced with the feed. If the gas were not subjected to a partial conversion of hydrogen and carbon monoxide into hydrocarbons the above would mean that 21.6 % of the feed energy would bece available in the form of cheap low BTU fuel gas, in addition to the energy in the form of hydrocarbon gas produced in the coking reactor (13.5 %w ClC4 hydrobons) which may also be used as a fuel gas. According to the invention the purified H2 and CO2 containing gas is contacted with a catalyst comprising 25 pbw of cobalt, 18 pbw of zirconium per 100 pbw of silica, which catalyst has been prepared by impregnation, and which catalyst has a 2 surface area of 100 mê/ml. The conversion is carried out at a temperature of 210 OC, a pressure of 20 bar and a space velocity 3 600 Nm COH2/Nm cat. hr. 3 of 600 Nm CO+H2/Nm cat. hr. of the Co and H2 in the feed, 55.9 % vol. are converted yielding 196 t/hr of liquid C5+ hydrocarbons and 346.103 Nm /her of a fuel gas having the following ccmposition: H2 5.66 % vol Co 21.09 N2 + others 72.12 C1-C4 1.13 The heating value of the gas is 4.1 MJ/Nm3. The gas production represents 396 MW, i.e. 11.7 % of the feed energy. The 19.6 t/hr C5+ hydrocarbons represent 242 MW, i.e. 7.1 % of the energy of the feed.

Claims: CLAIMS 1. Process for the preparation of hydrocarbons and a fuel gas fran a heavy carbonaceous teedstock, which process carprises: a) cracking the heavy carbonaceous feedstock in a coking zone which contains a bed of fluidized solids, producing hydrocarbons and coke which deposits upon the fluidized solids; b) introducing a part of the coke-cotaining solids into a gasification zone in which at least a part of the coke is gasified with an oxygen-containing gas, yielding a carbon moncxide- and hydrogen-containing gas mixture; c) partially converting the carbon monoxide- and hydrogen-con taining gas mixture into hydrocarbons in a synthesis zone; d) separating a tuel gas comprising carbon monoxide, hydrogen and gaseous hydrocarbons, and at least one liquid hydrocarbon fraction from the product of the synthesis zone. 2. Process as claimed in claim 1, in which the cracking process is a thermal process carried out at a temperature between 425 and 700 OC and a pressure between 1 and 15 bar. 3. Process as claimed in claim 1 or 2, in which the fluidized solids are coke particles. 4. Process as claimed in any one of claims 1-3, in which the solids are fluidized by means of steam as fluidizing gas. 5. Process as claimed in any one of claims 1-4, in which, the hydrocarbons produced in the coking zone are split up into at least one gaseous fraction and at least one liquid fraction. 6. Process as claimed in any one of claims 1-5, in which the coke-containing solids obtained from the coking zone are heated before being introduced into the gasification zone. 7. Process as clairred in claim 6, in which the coke-containing solids are heated in a fluidized bed by means of a hot fluidizing gas and/or hot fluidized solids. 8. Process as claimed in claim 7 in which the hot fluidizing gas is the carbon monoxide and hydrogen-containing gas obtained in the gasification zone, and the hot fluidized solids are solids frcm which the coke at least partially has been converted in the gasification zone. 9. Process as claimed in any one of claims 6-8, in which the coke containing solids are heated to a teeperature between 50 and 150 OC above the temperature of the coking zone at a pressure between 1 and 15 bar. 10. Process as claimed in any one of claims 1-9, in which in the synthesis zone the carbon mmide- and hydrogen-containing gas mixture is contacted with a catalyst comprising cobalt and at least one metal selected fran ruthenium, zirconium, titanium and chranium on silica, alumina or silica-alumina as carrier.

Inventors: SIE, SWAN TIONG
Applicants: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.
Application year: 1984
Main classification: C07C1
IPC codes: C07C1, C10G3, C10B55, C10G1, C10J3, C10G9, C10G2, C10G57