CN104774656A

CN104774656A - Process and apparatus for producing hydrocarbon fuel and composition

Info

Publication number: CN104774656A
Application number: CN201510114165.6A
Authority: CN
Inventors: J·F·麦吉; L·J·鲍尔
Original assignee: Universal Oil Products Co
Current assignee: Honeywell UOP LLC; Universal Oil Products Co
Priority date: 2009-12-11
Filing date: 2010-11-29
Publication date: 2015-07-15
Anticipated expiration: 2030-11-29
Also published as: EP2510076A4; EP2510076A2; CA2862613A1; CA2862613C; CN102652169A; WO2011071705A3; BR112012013470A2; SG178981A1; RU2517186C2; CA2773584C; CN104774656B; MX2012003049A; CA2773584A1; JP2016138277A; SG188922A1; JP2013513693A; RU2012129236A; CN102652169B; WO2011071705A2

Abstract

The present invention discloses a process and an apparatus for producing hydrocarbon fuel and composition. The process herein includes steps of: slurry hydrocracking a heavy hydrocarbon feed produces a HVGO stream and a pitch stream; at least a portion of the pitch stream is subjected to SDA to prepare a DAO stream low in metals; the DAO is blended with at least a portion of the HVGO stream to provide turbine or marine fuel with acceptable properties for combustion in gas turbines or for marine fuel grades.

Description

For the production of the method and apparatus of hydrocarbon fuel and composition

The divisional application of the application's to be application number be application for a patent for invention of 201080056121.8, the applying date of original application is on November 29th, 2010, and denomination of invention is: for the production of the method and apparatus of hydrocarbon fuel and composition.

The priority request of early stage national applications

This application claims the U. S. application Nos.12/636 being and submitting on December 11st, 2009,135; The right of priority of 12/636,137 and 12/636,142.

Invention field

The present invention relates to the method and apparatus for being prepared hydrocarbon fuel by slurry hydrocracking (SHC) and solvent deasphalting (SDA).

Description of Related Art

Because the reserves of conventional crude decline, heavy oil must be upgraded (upgrade) to satisfy the demands.During upgrading, heavier material converting become lighter fraction and most of sulphur, nitrogen and metal must be removed.Usually first in normal pressure crude still, process to provide by crude oil the fuel product comprising petroleum naphtha, kerosene and diesel oil.Usually obtaining normal pressure crude still bottoms flow to obtain vacuum gas oil (VGO) in vacuum tower, and described vacuum gas oil can be raw material or other purposes of FCC apparatus.VGO seethes with excitement usually in the scope of 300 DEG C of (572 ℉)-524 DEG C (975 ℉).

SHC is used for the heavy hydrocarbon feedstocks obtained by crude distillation, comprises the elementary upgrading of hydrocarbon residue or the gas oil distilled from atmospheric tower or vacuum distillation tower.In SHC, by these liquid starting materials and hydrogen and solid catalyst particle as particulate lithium compound as metallic sulfide mixes to provide slurry phase.Typical case's SHC method is such as described in US 5,755, and 955 and US 5,474, in 977.SHC method produces petroleum naphtha, diesel oil, gas oil as VGO, and low value refractory pitch stream.Usually being refined further in catalytic hydrocracking or fluid catalystic cracking (FCC) by VGO stream can sell goods to provide.For preventing transition coking in SHC reactor, heavy VGO (HVGO) can be made to be recycled in SHC reactor.

SDA usually refers to use and extracts in the presence of the solvent and the method for refining of such as above-mentioned hydrocarbon-fraction of upgrading.SDA allows actual recovered comparatively heavy oil under comparatively low temperature, and does not make crack heavier hydrocarbons or degraded.With distillation in volatility contrary, SDA by hydrocarbon according to they in liquid solvent solubleness separation.Lower molecular weight and more multichain alkane component are preferentially extracted.Minimum solvable material is high molecular and most polarity (most polar) aromatic component.

Internal combustion turbine has many purposes, comprises aero propulsion, generating and ship propulsion.Due to the development of internal combustion turbine material technology, burning zone temperature has improved hundreds of degree, allows the efficiency vast improvement in the circulation of Brighton.The internal combustion turbine of top efficiency can have the hot arc of operation more than 1093 DEG C (2000 ℉), therefore has and compares the much higher cycle efficiency of older generation's turbine.The internal combustion turbine of greater efficiency has produced the needs to tighter fuel specification.

According to article Svensson, DNV Approves Siemens Gas Turbine for HFO, 61 Royal Belgian Institute of Marine Engineers 55 (2007), 17MW type SGT-500 internal combustion turbine successfully stands comprehensive test, uses the oil fuel that meets IF180 specification and obtain Norway's government to approve about the DNV (Det Norske Veritas) of marine applications.When this article, IFO180 heavy fuel oil $ US200-250 more cheap than the intermediate oil usually burnt in marine gas turbine engine.IFO 180 specification is also referred to as RME 180 specification, and it is applicable to non-turbine machine as remaining bunker fuel used in the usual low RPM diesel engine found in ship system.

There are needs to this fuel because turbine than little to middle sizable application for generating, such as, for the peak power, more effective for fast boat other propulsion sources many as the ship propulsion of ferryboat, military transport ship and other application of electrical network.Reclaim the used heat of turbine to prepare steam or to provide the cogeneration plant of other low level heat to be realize high gross cycle efficiency, but need other example of the system of the fuel being suitable for turbine.

Previously made a lot of effort, prepared suitable gas turbine fuel by low value hydrocarbon residue.One method relates to hydroprocess petroleum residue, and wherein regularization condition is to remove sulphur and the nitrogen of only small portion, but most metals removes through catalyst for demetalation in " finishing method ".The example of the method is known as the GEFINERY of Japan Gasoline Corporation.Think that the cost of the method is high unreasonably based on limited upgrading limit.

Other method suggestion by hydrotreatment by dissolves from coal or " solvent treatment " coal product residue promote value (valorize) to produce decompression overhead product.The example of the method is the Hypercoal method of SRC (solvent refined coal) method and Japan New Energy Development Organization.In other method, make Residual petroleum stand SDA, the yield of wherein deasphalted oil (DAO) remains relatively low to avoid any organometallic compound to draw in DAO.The downstream purification of last a kind of methods combining SDA and DAO or hydrotreatment are removing metal.These three kinds of method examples are considered to disadvantageous, because their are produced, meet can suitable fuel limited in one's ability of application specification.

Specific fuel (for present subject matter) can be produced more cheap than typical marine diesel oil or kerosene.Even if because needs downstream contamination controls to remove SO from exhaust _xand NO _x, but it is favourable for fuel combustion this in turbine.

Current needs can be prepared and cheaply for the hydrocarbon fuel composition in internal combustion turbine and ship engine.

Summary of the invention

In typical embodiments, the present invention relates to the method preparing hydrocarbon fuel, described method comprise heavy feedstocks is carried out slurry hydrocracking to provide slurry hydrocracking product.Separating slurry isocrackate is to provide pitch stream and HVGO stream.Will at least partially pitch stream and solvent so that a part of pitch is dissolved in solvent.By the pitch of dissolving part with HVGO stream is blended to obtain blended product at least partially.In this respect, blended product comprises no more than 5wppm sodium, and no more than 50wppm vanadium and the blended product of at least 80 volume % are seethed with excitement at the temperature of 426 DEG C (800 ℉) or more.

In another typical embodiments, the present invention relates to the method preparing hydrocarbon fuel, described method comprise heavy feedstocks is carried out slurry hydrocracking to provide slurry hydrocracking product.Separating slurry isocrackate is to provide pitch stream and HVGO stream.Will at least partially pitch stream solvent deasphalting to provide DAO.By DAO with HVGO stream is blended to provide blended product at least partially.

In another typical embodiments, the present invention relates to the equipment preparing hydrocarbon fuel, described equipment comprises the slurry hydrocracking reactor reacting to produce slurry hydrocracking product for heavy feedstocks and hydrogen under catalyst action.The distillation stage be communicated with slurry hydrocracking reactor incites somebody to action slurry hydrocracking product fractionation at least partially.Distillation stage has side outlet for discharging HVGO stream or HVGO outlet and for the outlet at bottom that discharges pitch stream or asphalt outlet.Be communicated with SDA tower with asphalt outlet and produce DAO stream.It is from DAO outlet drain.With the container of side outlet and DAO outlet or pipeline will at least partially HVGO stream and DAO stream blended.

In another typical embodiments, this equipment comprises the separator for being separated from slurry hydrocracking product by hydrogen be communicated with SHC reactor.

In even another typical embodiments, the distillation stage of equipment also comprises the side outlet for discharging diesel stream and the side outlet for discharging light VGO (LVGO) stream.

In even another typical embodiments, the present invention relates to the compositions of hydrocarbons comprising and be no less than 73 % by weight aromatic hydrocarbons, no more than 5 % by weight heptane insolubles and no more than 50wppm vanadium.Seethe with excitement at the composition of at least 80 volume % temperature more than 426 DEG C (800 ℉).In other side, composition can comprise and be no less than 75 % by weight aromatic hydrocarbons, can comprise no more than 5 % by weight hexane undissolved substances or no more than 5 % by weight pentane insolubles.On the other hand, seethe with excitement at the temperature of the composition of at least 90 volume % more than 426 DEG C.On the other hand, composition has no more than 30wppm or no more than 10wppm vanadium.On the other hand, composition has the viscosity being not more than 180cSt at 50 DEG C.In another, composition has no more than 5wppm sodium.

These and other aspect that the present invention relates to and embodiment are learned by detailed description.

Definition

Term " aromatic hydrocarbons " is meant as measured the material comprised containing toroidal molecule by ASTM D 2549.

Term " connection " means operationally to allow that material flows between listed assembly.

Term " communicating downstream " means the material flowed at least partially in communicating downstream main body operationally can flow the main body be communicated with from it.

Term " upstream connection " means can operationally flow in the main body of its connection from the material of upstream connection main body at least partially.

As used herein, term " boiling temperature " means by the boiling temperature observed and distillation calculation of pressure, as the ASTM D1160 appendix A 7 that uses title be " Practice for Converting Observed VaporTemperatures to Atmospheric Equivalent Temperatures " the equivalent boiling point (AEBP) of normal pressure that calculates.

As used herein, " pitch " mean as by any standard gas chromatograph simulation distil method as ASTM D2887, D6352 or D7169 (it is all used by petroleum industry) measure boiling point at the hydrocarbon material of 538 DEG C of (975 ℉) more than AEBP.

As used herein, " bitumen conversion rate " means to be that the material converting of more than 524 DEG C (975 ℉) becomes boiling point at the transformation efficiency of 524 DEG C (975 ℉) or following material by boiling point.

As used herein, " heavy vacuum gas oil " mean as by any standard gas chromatograph simulation distil method as ASTM D2887, D6352 or D7169 (it is all used by petroleum industry) measure the hydrocarbon material of boiling point at 427 DEG C (800 ℉)-538 DEG C of (975 ℉) AEBP.

As used herein, solvent " insolubles " means to be insoluble to the material in described solvent.

Term " liquid hourly space velocity " means the volumetric flow rate of the liquid feeding of every reactor volume, and wherein solvent relates to the standard temperature of 16 DEG C.

Accompanying drawing is sketched

Accompanying drawing is the schematic diagram of the inventive method and equipment.

Detailed Description Of The Invention

Slurry hydrocrackingly can give the transformation efficiency many low value VACUUM TOWER BOTTOM product streams being changed into 524 DEG C (975 ℉) and the more 80-95 at the most % by weight of light distillate and a small amount of pitch.The Toluene Soluble part of the SHC product seethed with excitement under 524 DEG C (975 ℉) or higher temperature has relatively low molecular weight, such as, measure 700-900 according to ASTM D 2503 by vapour pressure osmometry, and by some nickel and pollution of vanadium.Slurry hydrocracking under ferrum-based catalyst effect under the following pressure of 20.7MPa (3000psig) have the limited capacity opening metalloporphyrin ring.Surprisingly, learn that the pentane soluble fractions of the asphaltic residue of boiling more than 524 DEG C from the transformation efficiency with more than 80 % by weight is slurry hydrocracking under ferrum-based catalyst effect contains low-down nickel and vanadium concentration.This is with the solubility organo-metallic nickel containing substantial amount and vanadium and the solvent deasphalting virgin oil that can not run in latest generation turbine is contrary.These fuel being loaded with metal only can use some technology such as metal passivation additive and off line water (offline water) washing to run in cooling turbomachine to remove blade deposit sediment.

Also learn and 524+ DEG C of residue is carried out slurry hydrocracking under ferrum-based catalyst effect by the transformation efficiency with more than 80 % by weight and most important part (being called HVGO) that the is vacuum gas oil overhead product seethed with excitement under 426-524 DEG C of (800-975 ℉) normal pressure equivalence boiling point of preparation does not comprise measurable nickel and vanadium.This material is also containing the paraffinic hydrocarbons within the scope of some C30-C45 and polycyclic aromatic hydrocarbons and heteroatoms material.This material has excellent fuel performance and at room temperature dumpable.Be suitable for directly burning as turbine fuel from the slurry hydrocracking comparatively light fraction (being called LVGO) of the vacuum gas oil overhead product of boiling in 343-426 DEG C of (650-800 ℉) normal pressure equivalence boiling spread, but this oil is escalated into petroleum naphtha in further processing with usual needs and diesel oil is better worth to give this stream.

Therefore, the HVGO obtained by SHC and the pitch of solvent deasphalting can be blended together to provide the hydrocarbon fuel meeting RME 180 and IFO 180 fuel specification.Therefore, hydrocarbon fuel can burn and not need further upgrading in internal combustion turbine and ship engine.The concrete composition of the hydrocarbon fuel prepared by the inventive method and equipment directly can be used or use with the blend mixed in batch with other fuel or the blend that mixes in use.

Embodiment of the present invention relate to be undertaken heavy hydrocarbon feedstocks slurry hydrocrackingly escalating into fuel with elementary.According to an embodiment, such as heavy hydrocarbon feedstocks comprises vacuum distillation tower residue.Other component of the representativeness of heavy hydrocarbon feedstocks is included in the residual oil of more than 566 DEG C (1050 ℉) boiling, tar, pitch earth, kerosene and shale oil.Pitch earth is also referred to as rock asphalt, Tar sands or oil-sand.Pitch earth is defined as the rock containing the hydrocarbon more more tacky than 10,000cSt, or this kind of hydrocarbon that can extract from exploitation or quarrying rock.Some natural bitumens are solid, such as gilsonite, grahamite and ceresine, and it is by the difference of striped, fusibleness and solubleness.Other asphaltenes-containibinders material also can be used as the component of being processed by SHC.Except asphaltene, heavy hydrocarbon feedstocks these other may component, in other attribute, in general manner also containing significant metal pollutant, the organosulfur of such as nickel, iron and vanadium, high-content and nitrogen compound, and Gao Kanglaxun carboloy residue.The metal content of this kind of component can be such as 100-1,000 weight ppm, and total sulfur content can be 1-7 % by weight, and api gravity can be-5 to 35 °.The Kang Laxun carboloy residue of this kind of component is at least 5 % by weight in general manner, is generally 10-30 % by weight.

As shown in drawings, for being become by converting heavy hydrocarbons the present invention of hydrocarbon fuel to be illustrated by SHC unit 10 and Solvent deasphalting unit 110.

Heavy feedstocks stream in pipeline 12 is shown as the charging of SHC unit 10 as shown in drawings.Heavy product recycle stream in pipeline 14 can be mixed with heavy feedstocks stream 12.Incoming flow in the granulated material of the coke suppressant additive in pipeline 16 or catalyzer and pipeline 12 is mixed to form homogenous slurry.Many kinds of solids granules of catalyst can be used as granulated material.Useful especially granules of catalyst is US 4,963, described in 247 those.Therefore, particle is generally the granularity that has and be less than 45 μm and on the one hand, major part, i.e. at least 50 % by weight ferrous sulfate with the granularity being less than 10 μm.FeSO4H2O is preferred catalyzer.Also can preferred bauxite catalyzer.On the one hand, granules of catalyst is suppressed to add in incoming mixture in the coke based on new raw material being 0.01-4.0 % by weight.Can be used as and select or use oil soluble coke suppressant additive in addition.It is metal naphthanates or the metal octoates of 50-1000wppm that oil soluble additive comprises based on the new raw material with molybdenum, tungsten, ruthenium, nickel, cobalt or iron.

The slurry of the catalyzer in pipeline 18 and heavy hydrocarbon charge can be mixed with the hydrogen in pipeline 20 and be transferred in fired heater 22 via pipeline 24.Combined feed is heated in well heater 22, is flowed in the entrance bottom tubular type SHC reactor 30 by source line 26.In well heater 22, the ferrum-based catalyst particle newly added from pipeline 16 transforms the iron sulphide being formed and have catalytic activity usually.In SHC reactor 30, there are some decompose.Such as, ferric sulfate monohydrate can change into Iron sulfuret and have when leaving well heater 22 and be less than 0.1 or the even granularity of 0.01 μm.SHC reactor 30 can take the three-phase without stationary solid bed as the form of solid-liquid-solid/liquid/gas reactions device, and catalyzer, the charging of hydrogen G&O move by wherein with pure moving upward, and have the back-mixing of some degree simultaneously.Other mixing many and pumping configuration can be suitable for charging, hydrogen and catalyst transport in reactor 30.

In SHC reactor 30, heavy feedstocks and hydrogen react to produce slurry hydrocracking product under the existence of above-mentioned catalyzer.SHC reactor 30 can operation and do not form coke under the pressure as mild as a dove within the scope of 3.5-24MPa.Temperature of reactor is generally 350-600 DEG C, the temperature of preferred 400-500 DEG C.LHSV is generally 4hr based on fresh feed ^-1below, preferred 0.1-3hr ^-1, particularly preferably 0.2-1hr ^-1.Bitumen conversion rate can be at least 80 % by weight, suitably at least 85 % by weight, preferably at least 90 % by weight.Hydrogen gas feed rate is 674-3370Nm ³/ m ³(4000-20,000SCF/bbl) oil.SHC is particularly suitable for the tubular reactor that charging and gas move upwardly through.Therefore, the outlet of SHC reactor 30 is at entrance top.Although only show one in accompanying drawing, one or more SHC reactor 30 can be used in parallel or in series.Due to the gas velocity raised, can bubble in SHC reactor 30.Also defoamer can be added in SHC reactor 30 to reduce the tendency producing foam.Suitable defoamer comprises as US 4, and 969, the silicone disclosed in 988.In addition, the hydrogen quenching material from pipeline 32 can be injected the top of SHC reactor 30 to cool slurry hydrocracking product when leaving reactor.

The slurry hydrocracking product stream comprising solution-airmixture is taken out by the top of pipeline 34 from SHC reactor 30.Slurry hydrocracking stream is made up of several product, comprises VGO and pitch, can be isolated with a large amount of different modes.By the slurry hydrocracking effluent at the top from SHC reactor 30 on the one hand under the separation temperature remaining on 200-470 DEG C (392-878 ℉), be separated in the high pressure hot separator 36 on the one hand under the pressure of SHC reaction.High pressure hot separator and SHC reactor 30 communicating downstream.Optional quenching material in pipeline 32 can help temperature required in reaction product quenching to high pressure hot separator 36.In high pressure hot separator 36, the effluent from SHC reactor 30 in pipeline 34 is separated into the air-flow comprising hydrogen and gasification product and the liquid stream comprising slurry hydrocracking product.Air-flow is the flash vaporized product under the temperature and pressure of high pressure hot separator.Equally, liquid stream is the flashed liquid under the temperature and pressure of high pressure hot separator 36.Air-flow is taken out by pipeline 38 at top from high pressure hot separator 36, liquid distillate is taken out by pipeline 40 in the bottom of high pressure hot separator 36 simultaneously.

Liquid distillate in pipeline 40 to be delivered in heat-lightening steaming pot 42 in the temperature identical with high pressure hot separator 36 under the pressure of 690-3,447kPa (100-500psig).Vapor overhead product in pipeline 44 to be cooled in water cooler 46 and the liquid bottoms product from cold high pressure separator in pipeline 48 is combined and enters in pipeline 50.Liquid distillate leaves heat-lightening steaming pot in pipeline 52.

Lower temperature is cooled in one or more water coolers that the overhead from high pressure hot separator 36 in pipeline 38 is represented at water cooler 54.Water washing (not shown) on pipeline 38 is generally used for washing out salt as curing ammonium or ammonium chloride.Water washing can remove nearly all ammonia and some hydrogen sulfide from the stream pipeline 38.Stream in pipeline 38 is delivered in the cold high pressure separator 56 with SHC reactor 30 and high pressure hot separator 36 communicating downstream.On the one hand, cold high pressure separator 56 in the temperature lower than high pressure hot separator 36, but operates at the same pressure.Under cold high pressure separator 56 remains on the temperature of 10-93 DEG C (50-200 ℉) and the pressure of SHC reactor 30.In cold high pressure separator 56, the top product of high pressure hot separator 36 is separated into the air-flow comprising hydrogen in pipeline 58 and the liquid stream comprising slurry hydrocracking product in pipeline 48.Air-flow is the flash vaporized cut under the temperature and pressure of cold high pressure separator 56.Equally, liquid stream is the flashed liquid product under the temperature and pressure of cold high pressure separator 56.By using this kind of separator, gained exit flow mainly containing hydrogen and some impurity as hydrogen sulfide, ammonia and light hydrocarbon gas.

Rich hydrogen stream in pipeline 58 can be passed through fills washing tower 60, it is washed by the washings in pipeline 62 to remove hydrogen sulfide and ammonia there.Renewable and the recirculation of spent scrub stream in pipeline 64, and be generally amine.The rich hydrogen stream of washing is discharged via pipeline 66 and is returned in SHC reactor 30 by circulating air compressor 68 and pipeline 20 recirculation from washer.Recycled hydrogen can be combined with the fresh supplemented hydrogen added by pipeline 70.

Liquid fraction in pipeline 48 is transported product liquid and in pipeline 44, is left the flash evaporation tank top product of the cooling of water cooler 46 to produce pipeline 50 with vicinity, described pipeline 50 the temperature identical with cold high pressure separator 56 and as heat-lightening steaming pot 42 in 690-3,447kPa (100-500psig) lower pressure under be fed into cold flash tank 72.Top gas in pipeline 74 for comprising the fuel gas of C4-material, can be reclaimed and utilized.The liquid bottoms product of the next self cooling flash tank 72 in pipeline 76 and flowing into separately in distillation stage 80 from the bottoms pipeline 52 of heat-lightening steaming pot 42.

Distillation stage 80 and SHC reactor 30 communicating downstream are to incite somebody to action described slurry hydrocracking product fractionation at least partially.Distillation stage 80 can comprise one or several container, although only show a container in figure.Distillation stage 80 can comprise atmospheric stripping separation column and reduced-pressure flash tank tower, but is only single vacuum distillation tower in one aspect.On the one hand, can by rare gas element as middle pressure steam feeds near bottom distillation stage 80 with the comparatively light constituent of stripping from heavy component in pipeline 82.Distillation stage 80 produce in pipeline 84 from top exit 83 discharge top gas product, pipeline 86 from side outlet 85 discharge naphtha products stream, pipeline 90 from side outlet 88 discharge diesel product stream, pipeline 92 from side outlet 91 discharge LVGO stream, pipeline 94 from side outlet 93 discharge HVGO stream and bottoms pipeline 98 from outlet at bottom 96 discharge pitch stream.

The SHC Asphalt Production logistics from outlet at bottom 96 in bottoms pipeline 98 is attached most importance to aromatic hydrocarbons and containing SHC catalyzer.Pitch seethes with excitement usually more than 524 DEG C (975 ℉).Separated from bitumen in pipeline 98 becomes enter the pipeline 100 of SDA unit 110 and return the pipeline 102 of SHC reactor 30 for recirculation.The HVGO product stream from side outlet in pipeline 94 is separated into for blended pipeline 106 and the pipeline 108 that returns for recirculation in SHC reactor 3.Stream in pipeline 102 and 108 can combine in pipeline 14.HVGO product stream seethes with excitement and is less than the boiling range of pitch more than 427 DEG C (800 ℉).The HVGO stream of at least 80 % by weight seethes with excitement more than 427 DEG C.On the other hand, the HVGO stream of at least 80 % by weight seethes with excitement below at 524 DEG C (975 ℉).Pipeline 106 transports at least partially from the HVGO stream of pipeline 94.

Asphalt material in pipeline 100 flows in SDA unit 110.In SDA method, to enter as the charging in pipeline 112 before in first extraction tower 120, the bitumen feed stream pumping in pipeline 100 is being mixed with the recirculation solvent in pipeline 116 and the supplementing solvent in pipeline 118.Can by other solvent, such as recirculation solvent adds the lower end of extraction tower 120 via pipeline 122.Light paraffinic hydrocarbon solvent, is generally a part of pitch in propane, butane, pentane, hexane, heptane or its mixture dissolution solvent.The pitch be dissolved in solvent rises to the top of tower 120.The decisive quality of the dissolving power of light hydrocarbon solvent is its density, so the solvent being equivalent to special solvent has equal density.Such as, in one embodiment, heptane is the densest solvent, and it can not promote the vanadium of high density and use in DAO.The solvent with the density lower than heptane is also suitable for the vanadium promoting (lift) low concentration in DAO.Specifically, the paraffinic hydrocarbons in dissolution with solvents bitumen feed and the aromatic substance of less polarity.Skellysolve A is suitable solvent.The heavier part of incoming flow 112 is insoluble and as the bituminous matter from asphalt outlet 123 in pipeline 124 or the sedimentation of pitch stream, and is extracted from the extracts of DAO outlet 127 discharge in pipeline 126 by a DAO stream.DAO stream in pipeline 126 is the pitch of dissolving part.Extraction tower 120 operates usually under 93-204 DEG C (200-400 ℉) and 3.8-5.6MPa (550-850psi).The temperature and pressure of extraction tower 120, but can more than stagnation point or below, condition controls density well usually below the stagnation point of solvent.DAO stream in pipeline 126 has the metal concentration lower than the incoming flow in pipeline 112.By a DAO stream in interchanger 128 and fired heater 129 or other interchanger by being heated to the supercritical temperature of solvent with the hot solvent indirect heat exchange in solvent recycled pipeline 136.The solvent of supercritical heated is separated with DAO in the DAO knockout tower 130 of the top communicating downstream with the first extraction tower 120.Solvent recycled stream leaves DAO knockout tower 130 in solvent recycled pipeline 136.Solvent recycled stream by interchanger 128 with the extract indirect heat exchange in pipeline 126 and condenser 154 and condensation.DAO knockout tower 130 operates usually under 177-287 DEG C (350-550 ℉) and 3.8-5.2MPa (550-750psi).Extractor bottom product stream in pipeline 124 contains the metal concentration larger than the charging in pipeline 112.Bottom product stream in pipeline 124 is heated in fired heater 140 or by other heat exchange method and in asphaltene stripper 150 stripping to obtain the lean solvent pitch stream in bottoms pipeline 152 and the first solvent recuperation stream in pipeline 134.Steam from pipeline 133 can be used as stripping liquid in asphaltene stripper 150.Asphalt outlet 123 communicating downstream of asphaltene stripper 150 and described solvent deasphalting tower 120 is with by solvent and separated from bitumen.Pitch stripper 150 operates usually under 204-260 DEG C (400-500 ℉) and 344-1,034kPa (50-150psi).Lean solvent DAO stream leaves DAO knockout tower 130 and enters and exports in the DAO stripping tower 160 of 127 communicating downstream with the bottom of DAO knockout tower 130 and described DAO in pipeline 132.DAO stripping tower 160 is by under low pressure by DAO stripping and being separated with DAO stream 132 by the second solvent recuperation stream 162 further from the solvent carried secretly.Steam from pipeline 163 can be used as stripping liquid in DAO stripping tower 160.DAO stripping tower 160 operates usually under 149-260 DEG C (300-500 ℉) and 344-1,034kPa (50-150psi).Second solvent recuperation stream is left and in the first solvent recuperation stream be attached to before in solvent tank 166 in pipeline 134 by water cooler 164 condensation and being stored in pipeline 162.Recovered solvent as required from storage tank 166 by pipeline 168 recirculation with the solvent made up line 136 to mix with the pitch stream in pipeline 100.In pipeline 172, provide substantially not solvent-laden DAO, it is at least partially from the DAO of DAO outlet 127 discharge.

By in pipeline 172 for the DAO of the dissolving part of pitch container as shown in the figure or pipeline 180 blended to provide blended product with the HVGO in pipeline 106, it has to comprise and is no less than 73 % by weight aromatic hydrocarbons, is preferably no less than the compositions of hydrocarbons of 75 % by weight aromatic hydrocarbons.Pipeline 180 or the container do not shown and HVGO side outlet 93, asphalt outlet 96 and DAO export 127 communicating downstream.Said composition can have no more than 5 % by weight heptane insolubles and no more than 50wppm vanadium.In another embodiment, compositions of hydrocarbons can have no more than 5 % by weight hexane undissolved substances and no more than 30wppm vanadium.In yet another embodiment, compositions of hydrocarbons can have no more than 5 % by weight pentane insolubles and no more than 10wppm vanadium.At least 80 volume %, preferably the composition of 90 volume % seethes with excitement at the temperature of 426 DEG C (800 ℉) or more.In one embodiment, compositions of hydrocarbons comprises no more than 3.5 % by weight sulphur, suitably no more than 1.0 % by weight sulphur, preferably no more than 0.5 % by weight sulphur.In another embodiment, blended compositions of hydrocarbons has the viscosity of no more than 180cSt at 50 DEG C and is not more than the molecular-weight average of 500.In one embodiment, compositions of hydrocarbons has the sodium of no more than 5wppm, preferred no more than 2wppm, so it can be suitable turbine fuel.

Embodiment

Carry out following examples to prove availability of the present invention.

Embodiment 1

Use SHC reactor is converted from Alberta with the bitumen conversion level of 80 and 90 % by weight, the asphaltic vacuum residuum of Canadian Peace River rock stratum.Be separated corresponding SHC product to provide bitumen product and HVGO product.The density of aromatic hydrocarbon of SHC product frac is measured by ASTM D2549-02 (2007) standard test methods (it is for being separated Typical Aromatic and the non-aromatics cut of high boiling point oil by elution chromatography).100% aromatic molecules is cosily rendered as under all transform levels of the pitch leaving SHC reactor more than 80 % by weight.The density of aromatic hydrocarbon measured for each HVGO cut provides in tablei.

Table I

SHC product	Transformation efficiency, % by weight	Boiling range, DEG C	Aromatic hydrocarbons, % by weight
				HVGO	80	425-524	71.3
HVGO	90	425-524	70.8
				Pitch	All	524+	100

Embodiment 2

Use SHC reactor is converted from Alberta with the bitumen conversion level of 87 % by weight, the asphaltic vacuum residuum of Canadian Peace River rock stratum.Be separated corresponding SHC product to provide bitumen product and HVGO product.Then bitumen product is made to stand to use Skellysolve A solvent and separated from solvent to extract DAO.Carry out blended calculating with the performance of the blend of the DAO of the HVGO product and extraction into heptane that measure compositions of hydrocarbons and selected ratio.Compared with RME180/IFO180 specification, the performance of blended compositions of hydrocarbons is shown in Table II.RME180/IF180 specification is shown to obtain 2:Requirements for Marine Residual Oils from iso standard 8217:2005 (E).In Table II, the density of aromatic hydrocarbon of blend measures as the weight average of the density of aromatic hydrocarbon in HVGO in Table I and pitch fractions.

Table II

Expect that all blends are based on according to Procedure 2B8.1 of the API PetroleumRefining Technical Handbook, its physicals of the 1st volume (1987) all has the pour point being less than 30 DEG C.According to API Petroleum Refining Handbook, program 2B2.1 in 1st volume (1987) and 2B2.3, HVGO is calculated: the blend that the ratio of pentane soluble asphalt equals 79:21 has the viscosity of 1201Cst, calculates HVGO: the blend that the ratio of pentane soluble asphalt equals 88:12 has the viscosity of 349cSt at the temperature of 30 DEG C.Therefore, all compositions in expection table be less than at 30 DEG C dumpable.

HVGO: the blend that the ratio of pentane soluble asphalt equals 79:21 is the prepared composition of SHC product.HVGO: the blend that the ratio of pentane soluble asphalt equals 85:15 has the viscosity specification met at 50 DEG C, but a little too dense and do not meet the composition of density specification.HVGO: the blend that the ratio of pentane soluble asphalt equals 88:12 has the composition meeting all RME180/IF180 specifications.

Measure HVGO: the blend that the ratio of pentane soluble asphalt equals 88:12 has and is less than 2wppm sodium.Expect that all blends have the na concn being less than 2wppm.

Embodiment 3

Use SHC reactor is converted from Peace River, Alberta with the bitumen conversion level of 87 % by weight, Canadian asphaltic vacuum residuum.Be separated corresponding SHC product to provide bitumen product.Bitumen product has the performance that Table III provides.

Table III

Asphalt density, g/cc	1.185
		Nickel, wppm	120
Vanadium, wppm	109

Then bitumen product is made to stand to use several solvents separated from solvent to extract DAO.Check the metal concentration of the pitch promoted by different solvents and density and be shown in Table IV.

Table IV

In this experiment, find that nickel in extraction oil and vanadium concentration and solvent density or % by weight yield are linear.In fact do not test hexane, but therefore performance pushes away in solvent density is between pentane and heptane.Surprisingly this little nickel and vanadium are present in the oil extracted by pitch.

Do not further describe, believe that those skilled in the art can use previous description, most integrated degree ground uses the present invention.Therefore, aforementioned preferred specific embodiments is interpreted as being only illustrative, and the rest part of limit publicity content never in any form.

In the preceding article, unless otherwise noted, all temperature are with a DEG C description, and all parts and percentage ratio are by weight.

In previously describing, those skilled in the art can easily determine principal character of the present invention, and make various changes and modifications of the present invention with can not departing from its spirit and scope be suitable for various uses and condition to make it.

Claims

1. compositions of hydrocarbons, it comprises:

Be no less than the aromatic hydrocarbons of 73 % by weight;

The no more than heptane insolubles of 5 % by weight; With

The vanadium of no more than 50wppm;

Wherein seethe with excitement at the temperature of the described composition of at least 80 volume % more than 426 DEG C (800 ℉).

2. compositions of hydrocarbons according to claim 1, it comprises the no more than hexane undissolved substance of 5 % by weight further.

3. compositions of hydrocarbons according to claim 1, it comprises the no more than heptane insolubles of 5 % by weight further.

4. compositions of hydrocarbons according to claim 1, it comprises further and is less than 10wppm vanadium.

5. compositions of hydrocarbons according to claim 1, wherein seethes with excitement at the temperature of the described composition of at least 90 volume % more than 426 DEG C (800 ℉).