EP0318694A2 - Process for the hydrogenation of solid carbon-containing feedstocks - Google Patents
Process for the hydrogenation of solid carbon-containing feedstocks Download PDFInfo
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- EP0318694A2 EP0318694A2 EP88117543A EP88117543A EP0318694A2 EP 0318694 A2 EP0318694 A2 EP 0318694A2 EP 88117543 A EP88117543 A EP 88117543A EP 88117543 A EP88117543 A EP 88117543A EP 0318694 A2 EP0318694 A2 EP 0318694A2
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
- C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
Definitions
- the invention relates to a process for the hydrogenation of solid carbonaceous feedstocks according to the preamble of claim 1. Temperatures in the bottom phase reactor of about 400 to 500 ° C and in the gas phase reactor of about 370 to 450 ° C are typical, and the process pressure can be between 150 to 1200 bar can be selected.
- a method is also known in which heavy oil is fed as a feed product to a preheater and in which a partial stream of the total amount of hydrogenation gas required, which is heated in a gas heat exchanger through which the hot separator head product flows, preheats the preheated mixture of heavy oil, additive and hydrogenation gas Entry into the bottom phase reactor is added (see. DE 35 23 709 Al).
- This process with separate hydrogenation gas heating had also already been proposed for coal hydrogenation (cf. DE 35 05 553 Al).
- the process-relevant parameters especially the defined inlet temperatures of the sump phase and gas phase reactors and the defined temperature in the intermediate separator - must be adjustable. These temperature settings are made more difficult by variable heat transfer rates due to contamination of the mash heat exchangers.
- the special conditions for the joint heating of mash and hydrogenation gas in the heat exchangers when driving with integrated gas phase hydrogenation must be taken into account; because it is known that there is an increased risk of drying out of the heat exchanger due to oil stripping by hydrogenation gas due to changed solvent quality.
- the exothermic heat of reaction from the sump phase and gas phase hydrogenation should be optimally used for heat recovery in order to achieve a heat-self-sufficient process or to keep the required additional heating small; the mash heating furnace should be avoided if possible, since this is one of the most critical components of any bottom phase hydrogenation.
- the defined process temperatures in the gas phase reactor and in the intermediate separator are set by means of external cooling, but without taking into account the heat recovery and the variable heat transfer performance of the mash heat exchanger due to increasing pollution.
- the increased risk of mash drying out in the heat exchangers is reduced by reducing the amount of hydrogenation gas in the mash heating path - the majority of the amount of hydrogenation gas is heated in separate gas heat exchangers; the setting of the two above So far, defined temperatures have not been taken into account.
- the two methods have the disadvantage that the heat exchanger for heating the liquid / solid gas mixture after the gas phase reactor - d. H. is arranged at a comparatively lower temperature level - and therefore no maximum heating of the liquid / solid gas mixture is guaranteed.
- the furnace for heating the liquid / solid gas mixture the so-called mash furnace, is reduced in capacity compared to the earlier hydrogenation processes, but it is not omitted.
- the object of the invention is to design the process sequence so that, firstly, the process-relevant temperatures in the gas phase reactor and in the intermediate separator can be set despite variable heat exchange performance of the mash heat exchangers, secondly, drying out of the mash in the mash heat exchangers is avoided and thirdly, the reaction heats of the bottom phase and gas phase hydrogenation a self-sufficient or thermally optimized process can be used.
- the defined temperature settings are made in the gas phase reactor and in the intermediate separator by gas heat exchangers with bypass operation, with indirect heat exchange taking place in the gas heat exchangers between the hot separator head product and the separately heated hydrogenation gas and the bypass being on the hydrogenation gas side.
- the separate gas heating also eliminates the risk of mash drying.
- the defined temperature setting in the gas phase reactor is also carried out according to the invention by a bypass on the mash heat exchanger on the hot separator head product side, which is arranged between the hot separator and the gas phase reactor, and by different feeds of vacuum gas oil on the path of the hot separator head product to the gas phase reactor.
- optimal mash heating is achieved in that, using the heat of reaction from the bottom phase and gas phase hydrogenation, the hot separator top product transfers its heat to the mash-hydrogenation gas mixture by indirect heat exchange at a respectively high temperature level and to the hydrogenation gas to be heated separately at a respectively lower temperature level.
- the hydrogenation gas furnace is then bypassed as a rule during normal operation and is only required for starting.
- the mash stream (3) is passed through three heat exchangers (18), (19), (20) and the hydrogen gas stream (5) to be heated separately before entering the hydrogenation gas oven (24) three heat exchangers (21), (22), (23) in countercurrent to the hot separator head product (9).
- the procedure can also be such that fresh hydrogen as a feed is provided for the mash stream and the cycle hydrogenating gas is provided for the second partial stream of the hydrogenation gas.
- stream (9) in the downstream direction comes into heat exchange relationship with the mash stream (3) in heat exchanger (20) and the partial stream of hydrogenation gas (5) in heat exchanger (23) and passes through a reactor (27) for hydrogenation in the gas phase at a fixed bed contact .
- the inlet temperature in the gas phase reactor (27) is, depending on the degree of contamination of the mash heat exchangers (18), (19) and (20), bypassing the heat exchangers (20) and (23) and via alternative vacuum gas oil feeds (32) in front of the heat exchangers (20) and ( 23) and by vacuum gas oil feed and quench gas feed in front of the gas phase reactor (27).
- the product stream refined in reactor (27) passes through stream (10) heat exchanger (19) and heat exchanger (22) in heat exchange relationship with stream (3) or stream (5) and one Intermediate separator (28) with separation of a hot oil fraction (11).
- the temperature in the intermediate separator (28) is set by bypassing in the heat exchanger (22).
- the residual stream (12) drawn off by the separator (28) gives off in the heat exchangers (18) and (21) its remaining heat, which can be used for heating the feed products, to stream (3) and stream (5) and is transferred via a water cooler (31).
- a gas scrubber can be provided in the usual way for working up the circulating hydrogen gas fraction. Such a work-up ensures a sufficient hydrogen partial pressure in the hydrogenation gas system by removing the C1 to C4 components which are soluble in the gas scrubbing by means of washing liquid.
- the separate partial stream from the total amount of hydrogenation gas to be used can make up 20 to 95, preferably 40 to 80% of the total amount of hydrogenation gas required.
- the defined temperature in the intermediate separator (28) is not via the gas heat exchanger (22) with bypass setting but set by means of the bypass procedure of the mash heat exchanger (19).
- a comparatively larger exchange surface is required for the mash heat exchanger (19); however, the gas heat exchanger (22) is omitted.
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Abstract
Description
Die Erfindung bezieht sich auf ein Verfahren zur Hydrierung fester kohlenstoffhaltiger Einsatzstoffe nach dem Oberbegriff von Patentanspruch 1. Hierbei sind Temperaturen im Sumpfphasereaktor von etwa 400 bis 500 °C und im Gasphasereaktor von etwa 370 bis 450 °C typisch, und der Verfahrensdruck kann zwischen 150 bis 1200 bar gewählt werden.The invention relates to a process for the hydrogenation of solid carbonaceous feedstocks according to the preamble of claim 1. Temperatures in the bottom phase reactor of about 400 to 500 ° C and in the gas phase reactor of about 370 to 450 ° C are typical, and the process pressure can be between 150 to 1200 bar can be selected.
Es sind Verfahren bekannt, wobei das gesamte Heißabscheiderkopfprodukt über eine nachgeschaltete Gasphasehydrierung gefahren wird und anschließend die Öle durch partielle Kondensation in einem Zwischenabscheider in der Weise aufgetrennt werden, daß der Lösungsmittelanteil als Zwischenabscheidersumpfprodukt direkt zur Kohlebreiherstellung rezirkuliert - sogenannte "direkte Lösungsmittelrückführung" - und die Nettoölprodukte als Zwischenabscheiderkopfprodukt (vgl. DE 35 24 449 Al und DE 30 22 158 Al) anfallen.Processes are known in which the entire hot separator top product is passed through a downstream gas phase hydrogenation and the oils are then separated by partial condensation in an intermediate separator in such a way that the solvent fraction as an intermediate separator bottom product recirculates directly to the production of coal slurry - so-called "direct solvent recycling" - and the net oil products as an intermediate separator top product (cf. DE 35 24 449 Al and DE 30 22 158 Al).
Es ist weiterhin ein Verfahren bekannt, bei dem Schweröl als Einsatzprodukt einem Vorheizer zugeführt wird und bei welchem ein in einem von dem Heißabscheiderkopfprodukt durchströmten Gaswärmetauscher aufgeheizter Teilstrom der insgesamt erforderlichen Hydriergasmenge dem vorgewärmten Gemisch von Schweröl, Additiv und Hydriergas vor Eintritt in den Sumpfphasereaktor zugegeben wird (vgl. DE 35 23 709 Al). Dieses Verfahren mit getrennter Hydriergasaufheizung war auch bereits für die Kohlehydrierung vorgeschlagen worden (vgl. DE 35 05 553 Al).A method is also known in which heavy oil is fed as a feed product to a preheater and in which a partial stream of the total amount of hydrogenation gas required, which is heated in a gas heat exchanger through which the hot separator head product flows, preheats the preheated mixture of heavy oil, additive and hydrogenation gas Entry into the bottom phase reactor is added (see. DE 35 23 709 Al). This process with separate hydrogenation gas heating had also already been proposed for coal hydrogenation (cf. DE 35 05 553 Al).
Bei der großtechnischen Realisierung eines Hydrierverfahrens mit Sumpfphase- und Gasphasehydrierung müssen drei Merkmale beachtet werden. Erstens müssen die prozeßrelevanten Parameter - speziell die definierten Eintrittstemperaturen von Sumpfphase- und Gasphasereaktor sowie die definierte Temperatur im Zwischenabscheider - einstellbar sein. Diese Temperatureinstellungen werden durch veränderliche Wärmeübertragungsleistungen infolge Verschmutzung der Maischewärmeaustauscher erschwert. Zweitens müssen die besonderen Bedingungen bei der gemeinsamen Aufheizung von Maische und Hydriergas in den Wärmeaustauschern bei der Fahrweise mit integrierter Gasphasehydrierung berücksichtigt werden; denn es ist bekannt, daß infolge veränderter Lösungsmittelqualität eine erhöhte Gefahr des Austrocknens der Wärmeaustauscher infolge Ölausstrippung durch Hydriergas besteht. Drittens soll die exotherme Reaktionswärme aus Sumpfphase- und Gasphasehydrierung in optimaler Weise für die Wärmerückgewinnung genutzt werden, um einen wärmeautarken Prozeß zu erreichen oder aber die erforderliche Zusatzheizung klein zu halten; es soll möglichst auf den Maischeaufheizofen verzichtet werden, da dieser eines der kritischsten Bauteile jeder Sumpfphasehydrierung darstellt.In the industrial implementation of a hydrogenation process with bottom phase and gas phase hydrogenation, three characteristics must be considered. First, the process-relevant parameters - especially the defined inlet temperatures of the sump phase and gas phase reactors and the defined temperature in the intermediate separator - must be adjustable. These temperature settings are made more difficult by variable heat transfer rates due to contamination of the mash heat exchangers. Secondly, the special conditions for the joint heating of mash and hydrogenation gas in the heat exchangers when driving with integrated gas phase hydrogenation must be taken into account; because it is known that there is an increased risk of drying out of the heat exchanger due to oil stripping by hydrogenation gas due to changed solvent quality. Thirdly, the exothermic heat of reaction from the sump phase and gas phase hydrogenation should be optimally used for heat recovery in order to achieve a heat-self-sufficient process or to keep the required additional heating small; the mash heating furnace should be avoided if possible, since this is one of the most critical components of any bottom phase hydrogenation.
Bei den bekannten Verfahren (z. B. o. g. DE 35 24 449 Al, DE 30 22 158 Al) werden mittels Fremdkühlung die definierten Prozeßtemperaturen im Gasphasereaktor und im Zwischenabscheider eingestellt, jedoch ohne Berücksichtigung der Wärmerückgewinnung sowie der veränderlichen Wärmeübertragungsleistungen der Maischewärmeaustauscher infolge zunehmender Verschmutzung.In the known processes (e.g. above DE 35 24 449 Al, DE 30 22 158 Al), the defined process temperatures in the gas phase reactor and in the intermediate separator are set by means of external cooling, but without taking into account the heat recovery and the variable heat transfer performance of the mash heat exchanger due to increasing pollution.
Bei den bekannten Verfahren (vgl. DE 35 23 709 Al und DE 35 05 553 Al) wird zwar die erhöhte Gefahr der Maischeaustrocknung in den Wärmeaustauschern durch Reduzierung der Hydriergasmenge im Maischeaufheizpfad - der große Teil der Hydriergasmenge wird in separaten Gaswärmeaustauschern aufgeheizt - reduziert; die Einstellung der beiden o. g. definierten Temperaturen blieb bisher unberücksichtigt. Die beiden Verfahren haben den Nachteil, daß der Wärmeaustauscher zur Aufheizung des Flüssig/Fest-Gasgemisches nach dem Gasphasereaktor - d. h. auf vergleichsweise niedrigerem Temperaturniveau - angeordnet ist und somit keine maximale Aufheizung des Flüssig/Fest-Gasgemisches gewährleistet ist. Somit ist zwar der Ofen für die Aufheizung des Flüssig/Fest-Gasgemisches, der sogenannte Maischeofen, in seiner Kapazität gegenüber den früheren Hydrierverfahren reduziert, er entfällt jedoch nicht.In the known processes (cf. DE 35 23 709 Al and DE 35 05 553 Al), the increased risk of mash drying out in the heat exchangers is reduced by reducing the amount of hydrogenation gas in the mash heating path - the majority of the amount of hydrogenation gas is heated in separate gas heat exchangers; the setting of the two above So far, defined temperatures have not been taken into account. The two methods have the disadvantage that the heat exchanger for heating the liquid / solid gas mixture after the gas phase reactor - d. H. is arranged at a comparatively lower temperature level - and therefore no maximum heating of the liquid / solid gas mixture is guaranteed. Thus, the furnace for heating the liquid / solid gas mixture, the so-called mash furnace, is reduced in capacity compared to the earlier hydrogenation processes, but it is not omitted.
Auch das bekannte Verfahren (vgl. DE 26 51 253 Al) erfüllt die o. g. Bedingungen nicht, da es sich nur auf die Sumpfphasehydrierung bezieht und der Maischeofen nicht entfallen kann.The known process (cf. DE 26 51 253 A1) does not meet the above-mentioned conditions, since it only relates to the bottom phase hydrogenation and the mash furnace cannot be omitted.
Die durch eine Mehrphasenströmung von Gasen und Dämpfen, Flüssigkeit sowie Feststoff im Rohr gekennzeichneten Verfahrensbedingungen ziehen erhebliche Unsicherheiten bei der Auslegung des Aufheizofens sowohl bei der Berechnung des Druckverlustes als auch des Wärmetransportes nach sich.The process conditions, which are characterized by a multi-phase flow of gases and vapors, liquid and solid in the tube, result in considerable uncertainties in the design of the heating furnace, both when calculating the pressure loss and the heat transfer.
Betriebstechnische Nachteile resultieren aus der Neigung zur Verkrustung der Innenseite der Ofenrohre und aus Verkokungsreaktionen des Produktes in den Rohren. Damit verbunden sind eine Laufzeitbegrenzung der Hydrieranlage insgesamt sowie auch sicherheitstechnische Probleme wie das Auftreten von sogenannten hot spots, die zu Rohrreißern führen können.Operational disadvantages result from the tendency to incrust the inside of the stove pipes and from coking reactions of the product in the pipes. This is associated with a limitation of the runtime of the hydrogenation system as a whole and also safety-related problems such as the occurrence of so-called hot spots, which can lead to pipe rips.
Die Erfindungsaufgabe besteht darin, den Verfahrensablauf so zu gestalten, daß erstens die prozeßrelevanten Temperaturen im Gasphasereaktor und im Zwischenabscheider trotz veränderlicher Wärmeaustauschleistung der Maischewärmeaustauscher eingestellt werden können, zweitens eine Austrocknung der Maische in den Maischewärmeaustauschern vermieden wird und drittens die Reaktionswärmen der Sumpfphase- und Gasphasehydrierung für einen wärmeautarken bzw. wärmetechnischen optimierten Prozeß genutzt werden.The object of the invention is to design the process sequence so that, firstly, the process-relevant temperatures in the gas phase reactor and in the intermediate separator can be set despite variable heat exchange performance of the mash heat exchangers, secondly, drying out of the mash in the mash heat exchangers is avoided and thirdly, the reaction heats of the bottom phase and gas phase hydrogenation a self-sufficient or thermally optimized process can be used.
Diese Aufgabe wird erfindungsgemäß dadurch gelöst, daß die Merkmale von Patentanspruch 1 verwirklicht sind.This object is achieved in that the features of claim 1 are realized.
Die definierten Temperatureinstellungen erfolgen im Gasphasereaktor und im Zwischenabscheider durch Gaswärmetauscher mit Bypaßbetrieb, wobei in den Gaswärmeaustauschern ein indirekter Wärmeaustausch zwischen dem Heißabscheiderkopfprodukt und dem getrennt aufgeheizten Hydriergas stattfindet und der Bypaß auf der Hydriergasseite ist. Durch die getrennte Gasaufheizung wird gleichzeitig die Gefahr der Maischeaustrocknung beseitigt. Die definierte Temperatureinstellung im Gasphasereaktor erfolgt weiterhin erfindungsgemäß durch einen heißabscheiderkopfproduktseitigen Bypaß am Maischewärmeaustauscher, welcher zwischen Heißabscheider und Gasphasereaktor angeordnet ist sowie durch unterschiedliche Einspeisungen von Vakuumgasöl auf dem Pfad des Heißabscheiderkopfproduktes zum Gasphasereaktor.The defined temperature settings are made in the gas phase reactor and in the intermediate separator by gas heat exchangers with bypass operation, with indirect heat exchange taking place in the gas heat exchangers between the hot separator head product and the separately heated hydrogenation gas and the bypass being on the hydrogenation gas side. The separate gas heating also eliminates the risk of mash drying. The defined temperature setting in the gas phase reactor is also carried out according to the invention by a bypass on the mash heat exchanger on the hot separator head product side, which is arranged between the hot separator and the gas phase reactor, and by different feeds of vacuum gas oil on the path of the hot separator head product to the gas phase reactor.
Gemäß der Erfindung wird eine optimale Maischeaufheizung dadurch erreicht, daß unter Ausnutzung der Reaktionswärme aus der Sumfphase- und Gasphasehydrierung das Heißabscheiderkopfprodukt seine Wärme durch indirekten Wärmeaustausch auf jeweils hohem Temperaturniveau an das Maische-Hydriergasgemisch und auf jeweils tieferem Temperaturniveau an das getrennt aufzuheizende Hydriergas überträgt. Hierdurch entfällt der Maischeaufheizofen und bei guter Wärmeisolierung auch ggf. der Hydriergasaufheizofen bei Normalbetrieb. Der Hydriergasofen wird dann in der Regel bei Normalbetrieb mittels Bypaß umfahren und nur zum Anfahren benötigt.According to the invention, optimal mash heating is achieved in that, using the heat of reaction from the bottom phase and gas phase hydrogenation, the hot separator top product transfers its heat to the mash-hydrogenation gas mixture by indirect heat exchange at a respectively high temperature level and to the hydrogenation gas to be heated separately at a respectively lower temperature level. This eliminates the mash heating oven and, if the insulation is good, the hydrogenation gas heating oven may also be omitted in normal operation. The hydrogenation gas furnace is then bypassed as a rule during normal operation and is only required for starting.
In weiterer Ausgestaltung (vgl. Fig. 1) des vorgeschlagenen Verfahrens werden der Maischestrom (3) durch drei Wärmetauscher (18), (19), (20) und der separat aufzuheizende Hydriergasstrom (5) vor Eintritt in den Hydriergasofen (24) durch drei Wärmetauscher (21), (22), (23) im Gegenstrom zu dem Heißabscheiderkopfprodukt (9) geführt.In a further embodiment (cf. FIG. 1) of the proposed method, the mash stream (3) is passed through three heat exchangers (18), (19), (20) and the hydrogen gas stream (5) to be heated separately before entering the hydrogenation gas oven (24) three heat exchangers (21), (22), (23) in countercurrent to the hot separator head product (9).
Bei der Aufteilung der Gesamt-Hydriergasmenge auf die beiden Teilströme kann auch so vorgegangen werden, daß für den Maischestrom Frischwasserstoff als Feed und für den zweiten Teilstrom des Hydriergases das Kreislaufhydriergas vorgesehen werden.When dividing the total amount of hydrogenation gas between the two partial streams, the procedure can also be such that fresh hydrogen as a feed is provided for the mash stream and the cycle hydrogenating gas is provided for the second partial stream of the hydrogenation gas.
Dabei tritt Strom (9) in Abstromrichtung nacheinander mit dem Maischestrom (3) in Wärmetauscher (20) und dem Teilstrom des Hydriergases (5) in Wämetauscher (23) in Wärmetauschbeziehung und durchläuft einen Reaktor (27) zur Hydrierung in der Gasphase an einem Festbettkontakt. Die Eintrittstemperatur im Gasphasereaktor (27) wird je nach Verschmutzungszustand der Maischewärmeaustauscher (18), (19) und (20) über Bypaßstellungen der Wärmeaustauscher (20) und (23) sowie über alternative Vakuumgasöleinspeisungen (32) vor die Wärmeaustauscher (20) und (23) sowie durch Vakuumgasöleinspeisung und Quenchgaseinspeisung vor den Gasphasereaktor (27) eingestellt. Der in Reaktor (27) raffinierte Produktstrom durchläuft als Strom (10) Wärmetauscher (19) und Wärmetauscher (22) in Wärmetauschbeziehung mit Strom (3) bzw. Strom (5) sowie einen Zwischenabscheider (28) mit Abtrennung einer Heißölfraktion (11). Die Temperatureinstellung im Zwischenabscheider (28) erfolgt durch Bypaßeinstellung im Wärmeaustauscher (22). Der von Abscheider (28) abgezogene Reststrom (12) gibt in den Wärmetauschern (18) und (21) seine restliche für die Aufheizung der Einsatzprodukte verwertbare Wärme an Strom (3) und Strom (5) ab und wird über einen Wasserkühler (31) einem Kaltabscheider (29) zugeführt, in dem eine Abtrennung von Abwasser (14) und Abgas sowie die Gewinnung einer Kaltölfraktion (13) und Rückführung des Kreislaufhydrierungsgasanteiles als Strom (15) über Kompressor (30) in den Prozeß erfolgen.In this case, stream (9) in the downstream direction comes into heat exchange relationship with the mash stream (3) in heat exchanger (20) and the partial stream of hydrogenation gas (5) in heat exchanger (23) and passes through a reactor (27) for hydrogenation in the gas phase at a fixed bed contact . The inlet temperature in the gas phase reactor (27) is, depending on the degree of contamination of the mash heat exchangers (18), (19) and (20), bypassing the heat exchangers (20) and (23) and via alternative vacuum gas oil feeds (32) in front of the heat exchangers (20) and ( 23) and by vacuum gas oil feed and quench gas feed in front of the gas phase reactor (27). The product stream refined in reactor (27) passes through stream (10) heat exchanger (19) and heat exchanger (22) in heat exchange relationship with stream (3) or stream (5) and one Intermediate separator (28) with separation of a hot oil fraction (11). The temperature in the intermediate separator (28) is set by bypassing in the heat exchanger (22). The residual stream (12) drawn off by the separator (28) gives off in the heat exchangers (18) and (21) its remaining heat, which can be used for heating the feed products, to stream (3) and stream (5) and is transferred via a water cooler (31). fed to a cold separator (29), in which a separation of waste water (14) and exhaust gas and the recovery of a cold oil fraction (13) and recycling of the cycle hydrogenation gas portion as stream (15) via compressor (30) take place in the process.
Im Anschluß an den Kaltabscheider (29) kann in üblicher Weise eine Gaswäsche zur Aufarbeitung des Kreislaufhydriergasanteiles vorgesehen werden. Durch eine derartige Aufarbeitung wird durch Entfernung der in der Gaswäsche mittels Waschflüssigkeit löslichen C₁- bis C₄-Bestandteile ein ausreichender Wasserstoffpartialdruck in dem Hydriergassystem gewährleistet.Following the cold separator (29), a gas scrubber can be provided in the usual way for working up the circulating hydrogen gas fraction. Such a work-up ensures a sufficient hydrogen partial pressure in the hydrogenation gas system by removing the C₁ to C₄ components which are soluble in the gas scrubbing by means of washing liquid.
Der separate Teilstrom aus der insgesamt einzusetzenden Hydriergasmenge kann 20 bis 95, vorzugsweise 40 bis 80 % der insgesamt erforderlichen Hydriergasmenge ausmachen.The separate partial stream from the total amount of hydrogenation gas to be used can make up 20 to 95, preferably 40 to 80% of the total amount of hydrogenation gas required.
In weiterer Ausgestaltung (vgl. Figur 2) wird die definierte Temperatur im Zwischenabscheider (28) nicht über den Gaswärmeaustauscher (22) mit Bypaßeinstellung sondern mittels Bypaßfahrweise des Maischewärmeaustauschers (19) eingestellt. Hierdurch wird zwar gegenüber Figur 1 eine vergleichweise größere Austauschfläche das Maischewärmeaustauschers (19) benötigt; es entfällt aber der Gaswärmeaustauscher (22).In a further embodiment (cf. FIG. 2), the defined temperature in the intermediate separator (28) is not via the gas heat exchanger (22) with bypass setting but set by means of the bypass procedure of the mash heat exchanger (19). As a result, compared to FIG. 1, a comparatively larger exchange surface is required for the mash heat exchanger (19); however, the gas heat exchanger (22) is omitted.
Claims (8)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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DE3741104 | 1987-12-04 | ||
DE19873741104 DE3741104A1 (en) | 1987-12-04 | 1987-12-04 | METHOD FOR HYDROGENATING SOLID CARBON-CONTAINING SUBSTANCES |
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Publication Number | Publication Date |
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EP0318694A2 true EP0318694A2 (en) | 1989-06-07 |
EP0318694A3 EP0318694A3 (en) | 1990-03-21 |
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Application Number | Title | Priority Date | Filing Date |
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EP88117543A Withdrawn EP0318694A3 (en) | 1987-12-04 | 1988-10-21 | Process for the hydrogenation of solid carbon-containing feedstocks |
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Country | Link |
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EP (1) | EP0318694A3 (en) |
JP (1) | JPH01172491A (en) |
DE (1) | DE3741104A1 (en) |
PL (1) | PL158461B1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN111849543A (en) * | 2020-07-08 | 2020-10-30 | 张家港保税区慧鑫化工科技有限公司 | Liquid phase hydrogenation feeding preheating system and process |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10032316A1 (en) * | 2000-07-04 | 2002-01-17 | Studiengesellschaft Kohle Mbh | Hydrogenation / hydrogenolysis of hard coal with borane catalysts |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0058327A2 (en) * | 1981-02-12 | 1982-08-25 | BASF Aktiengesellschaft | Process for the continuous preparation of hydrocarbon oils from coal by pressure hydrogenation |
EP0177676A2 (en) * | 1984-09-13 | 1986-04-16 | Ruhrkohle Aktiengesellschaft | Process carried out by heat recuperation for suspension hydrogenation with integrated gas phase hydrogenation |
DE3505553A1 (en) * | 1985-02-18 | 1986-08-21 | Veba Oel Entwicklungs-Gesellschaft mbH, 4650 Gelsenkirchen | METHOD FOR PRETREATING TREATMENT PRODUCTS FOR CARBON HYDROGENATION |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2936008A1 (en) * | 1979-09-06 | 1981-04-02 | Saarbergwerke AG, 6600 Saarbrücken | METHOD FOR HYDROGENATING COAL |
-
1987
- 1987-12-04 DE DE19873741104 patent/DE3741104A1/en not_active Withdrawn
-
1988
- 1988-10-21 EP EP88117543A patent/EP0318694A3/en not_active Withdrawn
- 1988-11-25 JP JP29636788A patent/JPH01172491A/en active Pending
- 1988-12-02 PL PL27616188A patent/PL158461B1/en unknown
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0058327A2 (en) * | 1981-02-12 | 1982-08-25 | BASF Aktiengesellschaft | Process for the continuous preparation of hydrocarbon oils from coal by pressure hydrogenation |
EP0177676A2 (en) * | 1984-09-13 | 1986-04-16 | Ruhrkohle Aktiengesellschaft | Process carried out by heat recuperation for suspension hydrogenation with integrated gas phase hydrogenation |
DE3505553A1 (en) * | 1985-02-18 | 1986-08-21 | Veba Oel Entwicklungs-Gesellschaft mbH, 4650 Gelsenkirchen | METHOD FOR PRETREATING TREATMENT PRODUCTS FOR CARBON HYDROGENATION |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN111849543A (en) * | 2020-07-08 | 2020-10-30 | 张家港保税区慧鑫化工科技有限公司 | Liquid phase hydrogenation feeding preheating system and process |
Also Published As
Publication number | Publication date |
---|---|
DE3741104A1 (en) | 1989-06-15 |
PL276161A1 (en) | 1989-07-24 |
JPH01172491A (en) | 1989-07-07 |
PL158461B1 (en) | 1992-09-30 |
EP0318694A3 (en) | 1990-03-21 |
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