EP3303521A1

EP3303521A1 - Method and device for separating asphaltenes from an asphaltene-containing fuel

Info

Publication number: EP3303521A1
Application number: EP16719358.0A
Authority: EP
Inventors: Sebastian LÖW; Markus Kinzl; Ralph Joh; Ansgar Kursawe; Herbert FAHRNBAUER; Thomas Fuchs; Jochen Petersen; Rüdiger Schneider; Nicolas Vortmeyer
Original assignee: Siemens AG
Current assignee: Siemens AG
Priority date: 2015-06-03
Filing date: 2016-04-21
Publication date: 2018-04-11
Also published as: US20180148655A1; WO2016192895A1

Abstract

The invention relates to a method for separating asphaltenes from an asphaltene-containing fuel (3), wherein the fuel (3) is supplied to a separation unit (5) in which a sub-stream (13) comprising low-boiling fuel components (15) of the fuel (3) is separated, wherein after separation of the sub-stream (13) the fuel (3, 19) is supplied to a deasphalting unit (7) in which asphaltenes contained in the fuel (3, 19) are separated by means of a solvent (23), wherein, after the separation of the asphaltenes from the fuel (3, 19), the solvent (23) is separated therefrom in a solvent recovery unit (9), wherein the separated solvent (23) is circulated back into the deasphalting unit (7), and wherein a solvent fraction (39) is obtained from the sub-stream (13) that has been separated from the fuel (3), which is supplied to the deasphalting unit (7) in addition to the solvent (23) recirculated from the solvent recovery unit (9). By means of a method of this type, a process-related solvent loss can be compensated in a simple and cost-effective manner via the targeted treatment of the asphalt-containing fuel. The invention further relates to a device (1, 51, 71) for carrying out a method of this type.

Description

description

Process and apparatus for separating asphaltenes from an asphaltene-containing fuel

The invention relates to a process for the separation of

Asphaltenes from an asphaltene-containing fuel. Furthermore, the invention relates to a corresponding device for the separation of asphaltenes from an asphaltene-containing fuel.

In the context of energy production is often on raw and

Heavy oils are used, which are available as low-cost fuels for energy production by gas turbines. However, such crude and heavy oils contain asphaltenes, which in turn contain chemically bound heavy metals. When the oils are burned, heavy metals such as vanadium or nickel are released as metal oxides. The metal oxides alloy with the metals of the turbine blades and corrode or weaken them.

Furthermore, regardless of their metal content, asphaltenes have the property of precipitating as a solid under severe pressure or temperature changes. These solid asphalt particles can clog pipes or fine nozzles of the burner used, and thus a lasting effect on the mixture formation in the turbine, thereby ge ^¬ will detract from the efficiency of the turbine. The combustion of crude oils in gas turbines is therefore subject to high requirements.

Light crude oils are only suitable for power generation in gas turbines, as modern high performance turbines heavy metal such as nickel or vanadium ^¬ le in the fuel only tolerate up to values which are below the concentration in most crude oils. For this reason alone, their use in heavy metal-sensitive high-performance turbines is prohibited. In addition, gas turbines of other classes are used. Although such gas turbines, which are operated at lower temperatures, lower efficiencies than the heavy metal-sensitive high-performance turbines. However, they are more tolerant of the heavy metals contained in crude and heavy oils. However, these heavy metal tolerant or vanadium insensitive standard turbines require an additive such as a magnesium salt to suppress the above-described corrosive effects of the heavy metals.

The use of a magnesium salt additive which is common as an inhibitor but forms a high-melting magnesium vanadate instead of low-melting vanadates. However, there is the risk of crusting on the turbine blades by layered deposition of the

Magnesium vanadate. To ensure the function of the turbine, the deposits or incrustations must be removed from the turbine blades, which requires a regular time-consuming and costly service effort. In particular, such a cleaning is associated with a turbine stoppage of several hours.

In order to separate the asphaltenes and the heavy metals from a entspre ^¬ sponding crude oil and thus render the crude oil for combustion in gas turbines, are so-called Deasphal- known tierungsverfahren. Deasphalting processes are based on extraction of asphaltenes by addition of saturated aliphatic hydrocarbons as precipitant or as solvent for the remaining oil constituents.

The heavy metals are strongly enriched in the asphaltenes, so that removal of the asphaltenes leads to an immediate removal of the heavy metals. By mixing the crude oil containing asphaltenes and heavy metals with the appropriate solvent, the asphaltenes are precipitated as a solid. The precipitated asphaltenes and the heavy metals removed during the precipitation of the asphaltenes then separated from the crude oil and thus removed from the process.

The preferred short-chain alkanes used as solvent (deasphalting agent) can be obtained after

However, do not completely separate the deasphalting from the purified asphaltene-containing fuel and return it to the deasphalting process. Common separation method such as a solvent evaporation in accordance with this established treatment units are generally ver ^¬ connected with losses of the separated solvent, since a complete separation comparable either for technical reasons not possible or very expensive is prevented. The non-separated solvent part thus remains in the stream of purified asphaltene-containing fuel and is burned with this in the gas turbine. Thus, an undesirable solvent loss must be accepted.

The invention is based, as a first object to provide a drive ^¬ Ver which allows by an efficient and inexpensive separation of asphaltenes from an asphaltene-containing fuel whose combustion in a Gasturbinenpro- process.

A second object of the invention is to specify a device by means of which such a method can be implemented in a correspondingly efficient and cost-effective manner.

The first object of the invention is achieved by a method for separating asphaltenes from an asphaltene-containing fuel, wherein the fuel is a Ab ^¬ separating unit is supplied, in which a partial stream with low-boiling fuel components is separated from the fuel, wherein the fuel after the Separation of the partial flow of a deasphalting unit is fed in the asphaltene contained in the fuel by means of a Lö- the solvent is separated after separation of the asphaltenes from the fuel in a solvent recovery unit, wherein the separated solvent is recycled to the Deasphal- tierungseinheit, and wherein the from

Part of the separated fuel stream, a solvent fraction is obtained which, in addition to the solvent ^recirculated from the solvent recovery unit,

Deasphaltierungseinheit is supplied.

In a first step, the invention is based on the consideration that due to the incomplete separation of the solvent used for deasphalting in the continuous process always solvent losses are recorded, so that the deasphalting as such in the worst case can not be completed and so not the desired cleaning effect can be achieved. Accordingly, to compensate for the solvent losses, a subsequent metering of the solvent in the deasphalting process is necessary.

However, due to the significantly higher cost of the solvents compared to the asphaltene-containing fuel, this increases the operating costs of the deasphalting process. Thus, for example, the operating costs for a gasoline fraction with comparatively low production costs of 0.5 € / L for refilling in a design for a 1000 MW power plant and an assumed solvent loss of 1% depending on the to be cleaned increase

asphaltene-containing fuel by about € 20 to 60 million / year. If more specialized solvent fractions, such as a pentane cut are needed for refilling, the costs incurred would be much higher.

Taking these considerations into account, the invention considers in a second step the composition of the asphaltene-containing fuels to be purified. When

Asphaltenhaltiger fuel is usually a crude oil used, in addition to the asphaltenes to be removed, ie contains the highly condensed aromatic hydrocarbons, especially a low molecular weight fraction of alkanes, alkenes and cycloalkanes. This fact now uses the invention in a third

Step and recognizes that the term be purified asphaltenhal- fuel itself useful for the recovery of solvent is ^¬ bar when a solvent fraction is recovered from the asphaltene-containing fuel, the Deasphal- tierungseinheit for separating the asphaltenes from the

Asphaltenhaltigen fuel is supplied.

In other words, the invention recognizes that it is possible to reduce the unwanted and unavoidable loss of solvent by the targeted treatment of the asphaltene-containing

Fuel in a simple and cost-effective manner auslei ^¬ Chen and substantially completely prevent this loss. When using short-chain alkanes as a solvent or as deasphalting a subsequent dosing or refilling completely eliminated because of the

asphaltene-containing fuel can be provided as such sufficient amounts of solvent, which compensate for the ^¬ loss of solvent. The solvent required for deasphalting is thus generated in the process itself, so that the cost of providing ^¬ position of the process metered solvent reduced to a minimum and avoided completely ideally. The preventable by applying the method Rückfüllkos- th will be a Deasphaltierungsprozess adapted to the on ^¬ requirements of a 1000 MW power plant, in a range between € / year and 60 million € 20 million / year.

The solvent required for deasphalting is guided between the Deasphaltierungseinheit and the solvent recovery unit continuously in the circuit, ie in a Lö ^¬ sungsmittelkreislauf. By supplying the separated ^¬ th solvent fraction to the solvent circuit is the circulating solvent constantly renewed. An Anrei ^¬ tion of unwanted secondary components and the resulting waste does not occur. The overall process thus does not require any waste stream and merely generates the stream of purified fuel that can be supplied to a gas turbine and the stream of separated asphaltenes, which can be used, for example, to produce high-quality road asphalt.

Furthermore, the process can be carried out under moderate process conditions. Supercritical and generally very ^high costs associated process conditions, such as in particular in the solvent recovery in the ROSE process, are not necessary. The fuel to be purified by asphaltenes is in particular a crude oil whose main constituents, in addition to asphaltenes (highly condensed aromatic hydrocarbons), are above all alkanes, alkenes, cycloalkanes. Besides still occur alipha ^¬ tables and heterocyclic nitrogen and Schwefelverbin- to fertilize.

The separation of the partial stream from the asphaltene-containing fuel to be cleaned takes place in the separation unit. In the present case, the first partial flow is understood as meaning the low-boiling fraction of the asphaltene-containing fuel, that is to say as a fraction with the low-boiling fuel constituents. This fraction is essentially free of heavy metals such as vanadium and nickel. The partial stream is expediently separated by distillation from the fuel.

In order to obtain the desired solvent fraction from the substream, the solvent fraction is distilled off from the substream by depletion of the substream. Here are from the partial stream, which corresponds to the total flow of the withdrawn low boilers, specifically separated those components as distillate, which are most suitable for the deasphalting. The distillate obtained is in the solution ^¬ medium circuit between the Deasphaltierungseinheit and solu- sungsmittelrückgewinnungseinheit dosed and flows zusätz ^¬ Lich to the circulating solvent in the

Deasphalting unit. Suitable solvents for deasphalting is insbesonde ^¬ re short-chain hydrocarbons, such as butanes (C4), pentanes (C5), hexanes (C6) and / or heptanes (C7). Butane (C4), pentanes (C5) and hexanes (C6), also referred to as C4-C6 fraction, are particularly preferably used. Accordingly, it is preferable to separate a solvent fraction from the partial stream containing C4-C6 carbons.

The solvent is used in the deasphalting to dissolve soluble constituents contained in the asphaltene-containing fuel, such as, for example, aliphatics, aromatics and paraffins. The asphaltene fraction (asphaltenes and heavy metals) contained in the asphaltene-containing fuel is insoluble in the solvent used so that the complementary and ^¬ tel is used with regard to the asphaltenes in a sense as an "anti-solvent".

In the separation of the first partial flow remains a

Bottom fraction, ie the fuel containing the high-boiling components and in particular all heavy metals and

Contains asphaltene. The fuel is thus concentrated on asphaltenes and heavy metals. This bottom fraction allows the separation of the asphaltenes and the fact angerei ^¬ cherten heavy metals. The fuel is supplied thereto zweckmäßi ^¬ reflect the amount of Deasphaltierungseinheit.

Here, the unequal distribution of heavy metals in the different fractions of these fuels is exploited: The heavy metals are largely in the so-called asphaltene fraction, which is defined as that of an oil which, when mixed with alkanes, typically propane, butane, Pentane, hexane or heptane, not dissolved by the added alkane. The

Asphaltenes stay behind as the second phase. This will allows the separation of the asphaltenes and the heavy metals enriched therein, with the heavy metal depletion levels usually ranging between 50% and 80%.

The solvent used for deasphalting is substantially made of Deasphaltierungseinheit starting from the Lö ^¬ sungsmittelrückgewinnungseinheit available. To ^¬ additionally to the recycled solvent, the solvent fraction obtained from the partial flow, a fraction which preferably butanes (C4), pentanes (C5) and hexanes (C6) is containing the Deasphaltierungseinheit supplied. In a partially adhere before ^¬ embodiment of the invention the solvent fraction of the Deasphaltierungseinheit is fed together with the recycled from the solvent recovery unit Lö ^¬ solvents. Both streams are pooled accordingly before entering the deasphalting unit.

After deasphalting be the te gereinig- of asphaltenes, ie the deasphalted fuel, and the complementary and ^¬ tel, conveniently supplied to the solvent recovery unit. Here, the solvent is purified and separated from the deasphalted fuel. The solvent is recycled to the deasphalting process. In addition to the recycled solvent, the solvent fraction obtained from the first part stream is the ^¬

Deasphaltierungsprozess supplied.

The asphaltenes separated from the fuel in the deasphalting unit are preferably drawn off and sent for further utilization.

After the separation of the solvent, the purified fuel is expediently fed to a gas turbine and burnt there to produce energy. Preferably, the depleted of the solvent fraction partial stream is fed to a gas turbine. In an advantageous embodiment of the invention, the purified fuel and the depleted partial stream are combined before the supply to the gas turbine. For this purpose, both streams are merged and fed together to the gas turbine. The union or the interference of the gaseous withdrawn

Streams, that of the depleted of the solvent fraction substream in the solvent recovery unit ver ^¬ lessening liquid Brennstoffström in a preferred embodiment after prior liquefaction of the partial stream by condensation. In this case, two liquid streams are combined and fed to a gas turbine for combustion ^¬ .

In a further preferred embodiment, the research is done Vermi- depleted of the solvent fraction part stream and the solvent recovery unit leaving ^¬ send Brennstoffström liquid in a quench apparatus. An advantage of such an association is that no condenser and no coolant supply are necessary. In the quenching apparatus of the gaseous depleted from the complementary and ^¬ telfraktion partial stream is brought into intimate contact with the liquid cleaned fuel. The gas is condensed by the liquid. The ^¬ de condensation heat are hereby remains free in the liquid mixture, so that its temperature rises slightly.

Furthermore, the energy previously used for the evaporation of the partial flow, which would again abge ^¬ leads in a condensation ^¬ and thus the system would be lost, held by the quenching in the system. The energy remains after the

Quenching in the total flow of fuel resulting from connection of streams. After quenching, this fuel stream thus has a correspondingly slightly higher temperature than the fuel leaving the solvent recovery unit before being combined.

In an alternative particularly preferred embodiment of the invention, the purified fuel and the exhausted cherte partial flow supplied to different turbines. Here, between standard turbines with high heavy metal tolerance (vanadium insensitive standard turbines) and so-called ^¬ ^'s High Performance Turbines with low heavy metal tolerance (vanadium-sensitive high performance turbines) is distinguished.

After separation of the solvent fraction from the first part of this stream is depleted of vanadium accordingly. In a particularly advantageous embodiment of the invention, the depleted of the solvent fraction first partial stream of a vanadium-sensitive high-performance turbine is supplied and there flows. There is no need for Addi ^¬ tive and there are also no turbine damage to be feared.

In other words, the vanadium-free low-boiling fraction, ie the abge ^¬ separated in the separation of the fuel part of energy, not only for the recovery of Deasphal- tierungsmittel, so the solvent fraction used son ^¬ countries can be efficiently radiates in a vanadiumempfind ^¬ union high performance turbine then ,

The purified fuel is preferably one

Vanadiumunempfindlichvanadiumtoleranten standard turbine supplied. Although residues of vanadium and / or heavy metals are still possible in this deasphalted fuel. However, these proportions are sufficiently low so that the combustion ^¬ material can be utilized energetically by a vanadium insensitive standard turbine.

The following describes the preparation and subsequent ^¬ sequent conversion into an asphalt-containing fuel is exemplified erläu ^¬ tert. A Brennstoffström is before entering a

Deasphalting unit preferably by distillation into a heavy metal-free fraction of low boilers ("top fraction") and an enriched in heavy metals high-boiling fraction ("bottom fraction") separated. The low-energy is here taken from the solvent fraction which is fed to the deasphalting process.

The high boiler, which are now concentrated in asphaltenes and heavy metals are subjected to the aid of the solution by means of a ^¬ Deasphaltierungsprozess. In this way the heavy metals are removed via the asphaltene fraction. As part of the deasphalting, depending on the process conditions, typically 2/3 to 3/4 of the heavy metals are removed. The expected in deasphalted fuel to ^¬ part of heavy metals here is by a

vanadium-insensitive standard turbine continues to exploit energe ^¬ table. Following the table the Aufberei ^¬ processing of a total asphalt-containing fuel stream 200 is exemplarily t / h explained in a proportion of 30 ppm of metals such as vanadium and nickel.

Fuel [t / h] vanadium [ppm]

Total fuel flow 200 (100%) 30

Low boilers 150 (75 o \

0} 0

High boiler 50 (25 o \

0} 120

Of which: Asphaltene 6 (12 o \

0} 700

DAO fraction 44 (88 o \

0} 36

Fuel usage (total) 194 (97%)

results from the mass balance

In the distillative separation of the total fuel stream (200 t / h) boiling about 75% (150 t / h) of the fuel as a vanadium-free, low-boiling overhead fraction. The remaining 25% (50 t / h) remain in addition to all heavy metals and asphalts as high boiler or sump fraction in the separation unit. The 75% low boilers, after separation of the desired solvent fraction in a vanadium-sensitive high-performance ^turbine can be efficiently ver ^¬ flows.

The high boiler, so the remaining 25% of the fuels is fes, contain a result of the separation of low-boiling part stream and the associated concentration of the bottoms fraction of a fraction of 12% (6 t / h corresponds to 3% be ^¬ subjected to the total current) and 120 ppm of heavy metals in the "swamp" and are fed to a deasphalting unit.

After deasphalting, a deasphalted fuel (DAO fraction) with vanadium content depleted by about 70% is recovered from the bottom fraction. Here, the asphaltenes (vanadium concentration about 700 ppm to 800 ppm) are removed from the fuel. The vanadium content results from the mass balance. There remain from the initial 25% of the asphalt-containing fuel with a Schwerme ^¬ tallkonzentration of 120 ppm about 22% of its mass as deasphalted and demetallized fuel with a vanadium concentration of 36 ppm.

The vanadium content of the deasphalted fuel is thus only slightly higher than the 36 ppm

Vanadiumanteil of the starting fuel with 30 ppm, and can still be energetically used by a vanadiumunempfindliche standard turbine.

In total, 97% of the fuel can be used in a targeted manner, with 75% of the fuel in one

vanadium-sensitive high-performance turbine are exuded. The remaining 22% of the fuel after separation of the asphaltenes and most of the heavy metals are processed in a vanadium-insensitive standard turbine. In total, almost 75% of additives can be saved, the service cost decreases almost proportionally.

The discharged 3% of asphaltenes are preferably subjected to secondary recycling such as bitumen, supplied as an aggregate for asphalt in road construction. Wei ^¬ terhin there is the advantageous possibility of the separated asphaltenes in a refinery an "upgrade" means

Blower / Coker subject to be recycled as a building material.

A separate power generation of the differently treated flows in the separation getrenn ^¬ th and the consequences so apply until the vanadium content in the deasphalted fuel exceeds the tolerance limit economic schwermetallto- leranter gas turbines.

Thus, about 75% of the fuel, or 70% to 72% remaining after separation of the solvent fraction, is emitted with high efficiency in a vanadium-sensitive high-performance turbine. Only the remainder of the fuel remaining after deasphalting of about 22% is emitted with a lower efficiency in a vanadium-insensitive standard turbine, which is only possible because of the relatively good vanadium tolerance of these turbines. Overall, as the größtmögli ^¬ che energetic benefit from an inserted

Asphaltenhaltigen fuel are drawn. Since very metal-containing fuels may still have high metal contents despite a deasphalting, the invention provides as a further alternative, the deasphaltierten fuel supply only so much of the heavy metal-free top fraction that the financial tolerance of service and additive costs of a vanadium-insensitive standard turbine is not exceeded. For this purpose, only part of the depleted of the solvent fraction substream prior to entry into a vanadium-insensitive standard turbine is combined with the deasphalted fuel. The remainder of the heavy metal-free top fraction then remains unchanged

supplied to vanadium-sensitive high-performance turbine. Thus, large parts of fuels, especially of light crude oils in vanadium-sensitive high-performance turbines without appreciable tolerance for heavy metals can be highly ^effluent ent.

An economically valuable Siedefrak ^¬ tion is more preferably separated from the fuel. An economically valuable boiling fraction is understood as meaning such a fraction or such a partial stream which contains components which, when economically exploited and / or sold, achieve a yield significantly above the calorific value of the fuel used. The separation of the boiling fraction is preferably carried out before the asphaltene-containing

Fuel to the deasphalting unit. Suitable for this purpose is the separation unit, in which the partial stream is withdrawn from the asphaltene-containing fuel to obtain the solvent fraction. In this process, a fraction of "medium boilers" is at ei ^¬ ner preferably carried out distillation withdrawn. This fraction is then fed to a WEI direct working up and can then be resold for profit.

Overall, targeted separation of an asphaltene-containing fuel in different (partial) flows, which is preceded by deasphalting, offers the possibility of efficiently and cost-effectively doing this for the

Deasphalting process needed to generate and use solvents in the ongoing process. In addition, the sub-flows that differ from each other in terms of their composition can be used specifically for use in a large-scale power plant with several turbines to be operated.

In this case, the robustness of a vanadium-insensitive standard turbine with respect to the contained high-boiling components of fuel fraction, that is the sump exploited bestmög ^¬ Lich and by the concentration of asphaltenes in the bottoms fraction of the best conditions for the Deasphaltierungsprozess created. At the same time, the high efficiency of a vanadium-sensitive high-performance turbine is achieved by the power generation of the partial flow with the low-boiling constituents.

The second object of the invention is inventively achieved by a device for the removal of asphaltenes from an asphaltene-containing fuel comprising a Deasphal- tierungseinheit for separating contained requested in the fuel asphaltenes by means of a solvent, a solution ^¬ medium recovery unit for separation of the solvent from the fuel, wherein the solvent recovery unit is flow ^¬ physically connected for returning the separated solvent to the Deasphaltierungseinheit, so-as comprising a with the Deasphaltierungseinheit flow ^¬ technically associated separating unit for separating a partial flow with low-boiling fuel components from the fuel, wherein the separation unit and the Deasphal ^¬ tierungseinheit such fluidically connected to one another are the that a recoverable from the separated part from the fuel stream ^¬ solvent fraction, in addition to that of the L solvent recovery unit recycled Lö ^¬ sungsmittel the deasphalting unit can be fed. Such a device allows through the fluidic connection of the separation unit and the Deasphaltierungs ^¬ unit to compensate for unwanted process-related solvent losses. The recoverable solvent fraction, which can be additionally fed to the deasphalting unit, avoids expensive replenishment or replenishment of solvent in the deasphalting process.

The Deasphaltierungseinheit is suitably connected a ^trailing conduit that is fluidly verbun to a supply of solvent recovery unit ^¬. The solvent recovery unit is zweckmä ^¬ ßigerweise also connected to a discharge line. These The discharge line is preferably fluidically connected to a return line of the deasphalting unit.

The interconnected lines thus form a solvent circuit between the deasphalting unit and the solvent recovery unit. In this complementary and ^¬ telkreislauf the solvent used for deasphalting circulated. The recoverable from the partial flow complementary and ^¬ telfraktion be supplied via this solvent circuit in addition to the circulating solvent of the deasphalting unit ^¬ and the Deasphaltierungsprozess.

Further advantageously, the Deasphaltierungseinheit is connected a ^trailing conduit for removal of the remote from the fuel in Deasphaltierungsprozess asphaltenes.

The separation unit upstream of the Deasphaltierungseinheit zweckmäßi ^¬ gerweise flow technology. In the separation unit, which is preferably designed as a distillation unit, a partial stream with low boilers is separated from the asphaltene-containing fuel.

For the withdrawal of the partial flow of the separation unit is preferably ei ^¬ ne discharge line connected. About the discharge line of the low-boiling components of the asphaltene-containing fuel containing partial stream is withdrawn, from which the solvent fraction is recovered. The solvent fraction is withdrawn from the substream. For deduction of the solvent fraction of the discharge line is preferably connected to an Ab branch line.

The branch line itself is advantageously flow ^¬-connected to a discharge of the solvent recovery unit. So one overall exploitable resources from the partial flow solvent fraction can be fed to the solvent circuit to ^¬ and correspondingly ge in Deasphaltierungseinheit ^¬ uses. The separation unit is advantageously fluidly connected to a gas turbine. This fluidic connection is expediently realized via the connection of the withdrawal line connected to the separation unit with a corresponding supply to the gas turbine. The depleted of the solvent fraction substream is fed according to the gas turbine and burned there. The same applies to the solvent recovery unit ^{leaving ¬} send of asphaltenes and solvents freed fuel. For combustion of the fuel, the complementary and ^¬ telrückgewinnungseinheit is expediently likewise strö ^¬ mung-connected to a gas turbine.

In an advantageous embodiment the solvent are recovery unit and the separating unit flow piercing ^¬ cally connected to the same gas turbine. The depleted of the solvent fraction substream and the fuel are preferably supplied here as a total flow of the turbine. For this, the discharge line of the disconnection is unit expediently with a drain line of Lö ^¬ sungsmittelrückgewinnungseinheit fluidic verbun ^¬.

In a particularly preferred alternative embodiment of the invention, the solvent recovery unit and the separation unit are fluidly coupled to different gas turbines. In particular, it is advantageous if the solvent recovery unit is fluidically connected to a vanadium-sensitive high-performance turbine. This possibility arises, the first part stream is essentially free of heavy metals, so that can be done a power generation without the addition of additives and without possible Turbinenbe ^¬ damage. The purified fuel is preferably one

vanadium-insensitive standard turbine is supplied.

For this, the solvent recovery unit zweckmäßi ^¬ gerweise fluidly with a vanadium-insensitive Standard turbine connected. If necessary, heavy metals still present in the fuel have no influence on their function because of the considerable higher heavy metal tolerance of vanadium-insensitive standard turbines compared to the vanadium-sensitive high-performance turbine.

In addition to the partial flow with the low-boiling constituents, an economically valuable boiling fraction can be separated from the asphaltene-containing fuel in the separation unit. To deduct such a fraction of the separation unit is expediently a discharge line connected ^¬ closed.

The advantages referred to preferred embodiments of the method can be transferred analogously to corresponding embodiments of the device.

In the following, embodiments of the invention will be explained in more detail with reference to a drawing. Show

1 shows a first device for the removal of

Asphaltenes from an asphaltene-containing fuel,

2 shows a second device for the removal of

Asphaltenes from an asphaltene-containing fuel

3 shows a third device for the removal of

Asphaltenes from an asphaltene-containing fuel

1 shows a device 1 for the removal of

Asphaltenes from an asphaltenhaltigen fuel 3 shown. The device 1 comprises a separation unit 5, one of the Ab ^¬ separation unit fluidly connected downstream Deasphaltierungseinheit 7, and a fluidically coupled to the Deasphaltierungseinheit 7 Solvent conditioning ^¬ unit. 9 The separation unit 5 is a total flow of 200 t / h of an asphaltenhaltigen fuel 3 via a supply line 11 is metered. Within the separation unit 5, which is presently designed as a distillation unit, a partial flow 13 with low-boiling components 15, the so-called top fraction, separated from the fuel 3 and deducted via a separation unit 5 connected to the exhaust line 17. The amount of withdrawn overhead fraction is 75 ~ 6, which corresponds to a fuel flow of 150 t / h. The head fraction 13 is free of vanadium.

In the separation unit 5, the asphaltenes remain

concentrated fuel 19. These are the high boilers containing 25% (50 t / h) of fuel 3 and 120 ppm of vanadium.

The concentrated fuel 19 containing 12% (corresponding to a flow of 6 t / h) of asphaltenes is supplied to the deasphalting unit 7 through a discharge pipe 21 connected to the separation unit 5. Here, the fuel 19 is purified of asphaltenes and heavy metals. Because the

Heavy metals are removed together with the asphaltenes, the withdrawal of 6 t of asphaltenes per hour together at the same time about 700 to 800 ppm of vanadium are removed from the fuel 19.

For this purpose, a solvent is used 23, which in ^¬ We sentlichen butanes (C4), pentanes (C5) and hexanes (C6) contains. The solvent 23 is used in the deasphalting for the solution of soluble constituents contained in asphaltene-containing fuel 19. The asphaltenes contained in the asphaltenhaltigen fuel 19 are insoluble in the solvent used 23, so that the solvent 23 is an "anti-solvent" with respect to the asphaltenes.

The separated asphaltenes and heavy metals are connected via ei ^¬ ne the Deasphaltierungseinheit 7 withdrawal line 24 of a present unspecified workup and subsequent recovery in accordance with this ausge ^¬ formed devices supplied. The deasphalted fuel 25 (DAO fraction) now still contains 36 ppm of vanadium and is fed together with the solvent to the solvent recovery unit 9. This is one of the

Deasphaltierungseinheit 7 connected discharge line 27 fluidly connected to a supply line 29 of the solvent recovery unit 9. In the solvent recovery unit ^¬ 9, the solvent is from 23

deasphalted fuel 25 separated and returned to the deasphalting process.

For recycling the solvent 23, the solvent ^¬ recovery unit 9 is connected a discharge line 31, which fluidly connected to a return line 33

Deasphaltierungseinheit 7 is connected. Via these lines 27, 29, 31, 33, the solvent 23 circulates between the deasphalting unit 7 and the solvent recovery unit 9 in a solvent circuit 35.

The separation of the solvent 23 in the solvent ^¬ recovery unit 9 is generally associated with losses. A portion of the solvent portion 23 remains in the stream of purified fuel 25 and is burned with this in a solvent recovery unit 9 connected gas turbine ^¬ 37. This undesirable Lösungsmittelver ^¬ loss must be compensated.

For this purpose, the separated in the separation unit 5 from the fuel asphalted tenhaltigen 3 partial stream is used with 13 easily ^¬ boiling components 15th From the partial stream 13, a solvent fraction 39 is separated by distillation. Here, from the partial stream 13 which corresponds to the total flow of the removed low-boiling components, specifically those components separated as a distillate, which are suitable for the deasphalting bes ^¬ th. In the present case, a C4 / C5 / C6 fraction 39 is separated from the partial flow 13. The distillate 39 obtained is metered into the solvent circuit 35 between the Deasphaltierungseinheit 7 and the complementary and ^¬ telrückgewinnungseinheit 9 and flows in addition to the recirculated 35 solvent 23 in the

Deasphalting unit 7 a. The discharge line 17 of the Ab ^¬ separation unit 3 is for this purpose a branch line 41 is Schlos ^¬ sen, which is in turn fluidly connected to the discharge line 31 of the solvent recovery unit 9 and with the rear ^¬ conduit 33 of the Deasphaltierungseinheit. 7

By adding the solvent fraction 39 to the circulating solvent 23, it is possible to dispense with replenishment and thus to minimize the costs for the spreading of the solvent 23 required for the deasphalting.

Both the solvent recovery unit 9, as well as the separation unit 3 are fluidly connected to the gas turbine 37. For this purpose, the depleted from the solvent fraction 39 gaseous partial stream is combined with the solution 13, the medium ^¬ recovery unit 9 exiting liquid fuel ^¬ material flow 25th Here, the gaseous part ^¬ stream 13 prior to combining liquefied first, to which a cooler is angeord- net 43 in the discharge line 17 of the separation unit. 5 Thus, two liquid streams 13, 25 are combined and then jointly supplied to the gas turbine 37 for combustion.

For admixing the liquefied after the condensation partial flow 13, the discharge line 17 of the separation unit 5 is fluidly connected to a discharge line 45 of the solvent recovery unit 9.

Overall, the method and the apparatus 1 used to allows its implementing the targeted treatmen ^¬ development of asphalt-containing fuel to generate the 3 needed for the solvent deasphalting 23, 39, so that the cost for the provision of the solvent 23 a minimum is reduced and ideally avoided altogether.

FIG. 2 shows a further device 51 for removing asphaltenes from an asphaltene-containing fuel 3. In this case, the device 51 is designed substantially like the device 1 according to FIG. 1.

The feasible with the device 51 The method, as well as the individual apparatus components corresponding to those of the device 1 according to FIG 1. Thus, the device 51 includes the separating unit 5, which the separating strö ^¬ mung technically downstream Deasphaltierungseinheit 7 so ^¬ as with the Deasphaltierungseinheit fluidically coupled solvent treatment unit 9. Accordingly, the detailed description of Figure 1 can be transmitted to the Vorrich ^¬ tung 51 of FIG. 2

The essential difference between the two devices 1, 51 lies in the combination of the depleted of the solvent fraction 39 substream 13 and the asphaltenes purified, separated in the solvent processing unit 9 from the solvent 23 fuel 25. The device 51 herein comprises instead of a cooler, as it is inserted in the device 1 according to FIG 1, a quenching apparatus 53. the quench apparatus 53 is attached ^¬ belongs to the Ab ^¬ zugsleitung 45 of the solvent recovery unit. 9 The mixing of the depleted of the solvent fraction 39, gaseous substream 13 and the Lö ^¬ sungsmittelrückgewinnungseinheit 9 leaving liquid fuel stream 25 is carried out directly in a quenching apparatus. With such a direct union no cooler is necessary.

In addition, the separating unit 5 comprises a further trigger ^¬ line 55 via which an economically valuable Siedefrakti ^¬ on 57, in this case with aromatic components 59, from the Asphaltenhaltigen fuel 3 is subtracted. This boiling ^¬ fraction 57 is recovered as a medium-boiling fraction, the aromatics contained then fed to a presently unspecified ge ^¬ showed work-up and then can be sold at a profit.

FIG. 3 shows a device 71 which is likewise used to separate asphaltenes from the asphaltene-containing fuel 3. Again, the separation unit 5, the Deasphaltierungseinheit 7, and the solution inflow preparation ^¬ processing unit 9 are used, so that it can be made to the devices 1, 51 according to FIGS 1 and 2 with regard to the detail ^¬ profiled description. The main difference from the Figures 1 and 2 lies in the combustion of the sub-stream 13 and the fuel 25. Before ^¬ lying the purified fuel 25 and the partial flow is 13-assured abgerei- different turbines 73, 75, respectively.

This possibility is provided because of the different ^¬ together mensetzungen the respective currents 13, 25th Since the partial flow 13 contains only low-boiling constituents 15 and no heavy metals or asphaltenes, it can be emitted in a vanadium-sensitive high-performance turbine 73. It requires no additives and there are also no turbine damage to be feared.

In other words, the vanadium-free low-boiling fraction, that is to say the partial stream 13 separated off from the fuel 3 in the separation unit 5, is not only used for obtaining

Deasphaltierungsmittel, so the solvent fraction 39, used, but can then efficiently in a

vanadium-sensitive high-performance turbine 73 are exuded.

The purified fuel 25 becomes one

vanadium-insensitive standard turbine 75 supplied. There are Residues of vanadium and / or heavy metals are still possible in this deasphalted fuel. However, these proportions are sufficiently low, so that the fuel 25 can be energetically utilized by a vanadium-insensitive standard turbine 75.

Such a separate power generation of the separated in the separation unit 3 and subsequently treated differently streams 13, 25 is applicable until the

Vanadiumanteil in the deasphalted fuel 25 exceeds the turbines ^¬ specific heavy metal tolerance limit. If this is the case, it is possible to meter a low-boiling part 77 of the partial flow 13 to the fuel 25, so that the economic tolerance limit is not exceeded by service and additive costs of the vanadium-insensitive standard turbine 75.

Accordingly, the portion 77 of the depleted of the solvent fraction 39 substream 13 before entering the fuel 25 in the vanadium insensitive standard turbine 75 is combined with this. The discharge line 17 of the Ab ^¬ separation unit 5 and the discharge line 45 of the solvent recovery unit ^¬ 9 are for this purpose fluidly connected to each other via a Kopplungslei ^¬ tung 79th This Kopp- development line 79 is never identified in FIG 3 as an option as dashed Li ^¬. The remainder of the partial flow 13 remaining after the separation of the low-boiling part 77 is fed to the vanadium-sensitive high-performance turbine 73 as described above and is burned there with high efficiency.

Overall, by means of a separation unit 5 arranged upstream of the deasphalting unit 7 and the associated possibility of a targeted separation of an asphaltene-containing fuel 3 in different (partial) streams 13, 25, it is possible in an efficient and cost-effective manner to selectively use the solvent required for the deasphalting process 23, 39 in the ongoing process to generate and use. In addition, the different from each other in terms of their composition sub-streams 13, 25 can be targeted for use in a large power plant with multiple turbines to be operated, such as a vanadium-sensitive high-performance turbine 73 and a vanadium insensitive standard turbine 75.

Claims

claims

A process for separating asphaltenes from an asphaltene-containing fuel (3), wherein the fuel (3) is supplied to a separation unit (5) in which a partial flow (13) with low-boiling fuel components (15) is separated from the fuel (3) , wherein the fuel (3, 19) after the separation of the partial flow (13) of a

Deasphaltierungseinheit (7) is supplied, in the fuel (3, 19) contained asphaltenes are separated by means of a ^{Lösungsmit ¬} means (23), wherein the solvent (23) after the separation of the asphaltenes from the fuel (3, 19) in a solvent recovery unit (9) is separated therefrom, wherein the separated solvent (23) is returned to the Deasphaltierungseinheit (7), and wherein from the separated from the fuel (3) partial stream (13) a solvent fraction (39) is recovered, which in addition to the solvent (23) recycled from the solvent recovery unit (9)

Deasphaltierungseinheit (7) is supplied.

2. The method of claim 1, wherein the partial stream (13) with low-boiling fuel components (15) by distillation from the fuel (3) is separated.

3. The method according to claim 1 or 2, wherein the solvent fraction (39) by distillation under depletion of the partial stream (13) is separated therefrom.

4. The method of claim 3, wherein the depleted from the solvent fraction (39) partial stream (13) of a Gasturbi ^¬ ne (37, 73, 75) is supplied.

5. The method according to any one of the preceding claims, wherein the purified fuel (25) after the separation of the Lö ^¬ sungsmittels (23) of a gas turbine (37, 73, 75) is supplied.

6. The method according to any one of the preceding claims, wherein the purified fuel (25) and the depleted part ^¬ stream (13) before supply to the gas turbine (37, 73, 75) verei ^¬ nigt.

7. The method according to any one of claims 1 to 5, wherein the depleted substream (13) of a vanadium-sensitive high-performance turbine (73) is supplied.

8. The method according to any one of claims 1 to 5 and 7, wherein the purified fuel (25) of a vanadium insensitive standard turbine (75) is supplied.

9. The method according to any one of the preceding claims, wherein an economically valuable boiling fraction (57) from the fuel (3) is separated.

10. Device (1, 51, 71) for the removal of asphaltenes from an asphaltene-containing fuel (3) comprising a Deasphaltierungseinheit (7) for separating in the fuel (3, 19) asphaltenes contained by means of a solution ^¬ means (23), a solvent recovery unit (9) for separating the solvent (23) from the fuel (3, 19), the solvent recovery unit (9) for recirculating the separated solvent (23) being fluidly connected to the deasphalting unit (7), and um ^¬ grasping a separation unit (5) ^fluidically connected to the deasphalting unit (7) for separating a partial flow (13) with low-boiling fuel components (15) from the fuel (3), wherein the separation unit (5) and the deasphalting unit (7) are fluidically connected to one another are connected, that a recoverable from the fuel (3) partial flow (13) recoverable solvent fraction (39) zusä in addition to the solvent (23) recycled from the solvent recovery unit (9)

Deasphaltierungseinheit (7) can be fed.

11. Device (1, 51, 71) according to claim 10, wherein the separating unit (5) of the deasphalting unit (7) is ^fluidically technically upstream.

12. Device (1, 51, 71) according to claim 10 or 11, wherein a distillation unit is used as a separation unit (5).

13. Device (1, 51, 71) according to any one of claims 10 to 12, wherein the separating unit (5) has a discharge line (17) for

Discharge of the partial flow (13) is connected.

14. Device (1, 51, 71) according to claim 13, wherein the discharge line (17) is connected to a branch line (41) for withdrawing the solvent fraction (39).

15. Device (1, 51, 71) according to claim 14, wherein the branch line (41) is fluidly connected to a discharge line (31) of the solvent recovery unit (9).

16. Device (1, 51, 71) according to one of claims 10 to

15, wherein the separation unit (5) is fluidly connected to a gas turbine (37, 73, 75).

17. Device (1, 51, 71) according to one of claims 10 to

16, wherein the solvent recovery unit (9) is Strö ^¬ ment technically connected to a gas turbine (37, 73, 75).

18. Device (1, 51, 71) according to one of claims 10 to

17, wherein the solvent recovery unit (9) and the separation unit (5) are fluidly connected to the same gas turbine (37, 73, 75).

19. Device (1, 51, 71) according to any one of claims 10 to 17, wherein the separating unit (5) fluidly with a vanadium-sensitive high-performance turbine (73) is connected.

20. Device (1, 51, 71) according to any one of claims 10 to 17 and 19, wherein the solvent recovery unit (9) is fluidly connected to a vanadium insensitive standard turbine (75).

21. Device (1, 51, 71) according to any one of claims 10 to 20, wherein the separating unit (5) has a discharge line (55) for

Deduction of an economically valuable boiling fraction (57) from the fuel (3) is connected.