CN101316983A - Methods of filtering a liquid stream produced from an in situ heat treatment process - Google Patents

Abstract

The invention provides a method for producing one or a plurality of crude oil products, comprising: producing the stratum fluid by a underground situ heat treating method; separating the stratum fluid, producing the liquid material flow and a gas material flow; providing at least part of the liquid material flow to a nanofiltration system, producing liquid both getting through the membrane and not getting through it, providing the liquid both getting through the membrane to one or plurality of processing units at the downstream of the nanofiltration system; and processing the filtered liquid material flow in one or a plurality of process units at the downstream, to form one or a plurality of crude oil products.

Description

Filtration is by the method for the liquid stream of situ heat treatment method production

Technical field

Relate generally to of the present invention by various subsurface formations for example hydrocarbon containing formation produce the method and system of hydrocarbon, hydrogen and/or other products.

Background technology

The hydrocarbon that from subsurface formations, obtains usually as the energy, as raw material with as the consumer goods.The worry that obtainable hydrocarbon source is exhausted and the worry that the gross mass of the hydrocarbon produced descends caused having developed the method for gathering more effectively, processing and/or using obtainable hydrocarbon source.Can use in-situ method from subsurface formations, to shift out hydrocarbon materials.May need to change the chemistry and/or the physical property of the hydrocarbon materials in the subsurface formations, from subsurface formations, shift out more easily to allow hydrocarbon materials.Chemistry and physical change can comprise the reaction in-situ of the viscosity variation that produces extensible fluid, forms hydrocarbon materials in variation, changes in solubility, variable density, phase transformation and/or the stratum.Fluid can be but be not limited to gas, liquid, emulsion, slurry and/or have logistics with the solid particle of the similar flow performance of liquid flow.

The formation fluid that uses the situ heat treatment method to obtain from subsurface formations can be sold and/or be processed to produce commercial product.The formation fluid of producing by the situ heat treatment method can have and different performance and/or the compositions of formation fluid that obtains by conventional production method.The formation fluid that uses the situ heat treatment method to obtain from subsurface formations may not satisfy transportation and/or the commercial industrial standard of using.Therefore, need to handle improving one's methods and system of the formation fluid that from various hydrocarbon containing formations, obtains.

Summary of the invention

The processing method of the formation fluid that embodiment relate generally to described herein is produced from subsurface formations.

In some embodiments, the invention provides the method for producing one or more crude oil products, this method comprises: by underground situ heat treatment method grown place layer fluid; Layer fluid is produced liquid stream and gas stream discretely; Provide partially liq logistics at least to the feed side of the film of filtration system, produce seepage remaining liquid and penetrating fluid, wherein seepage remaining liquid comprises the occlusion group compound; With one or more processing unit for processing penetrating fluids, to form one or more crude oil products in the nanofiltration system downstream.

In some embodiments, the invention provides the method for producing alkylated hydrocarbons, this method comprises: by underground situ heat treatment method grown place layer fluid; Layer fluid is produced liquid stream discretely; In first catalytic cracking system, catalytic cracking partially liq logistics at least is to produce crude oil products; Near small part crude oil products is separated into one or more hydrocarbon streams, and wherein at least a hydrocarbon stream is the gasoline hydrocarbon logistics; In second catalytic cracking system, catalytic cracking is produced thick olefin stream to the logistics of small part gasoline hydrocarbon by contacting gasoline hydrocarbon logistics and catalytic cracking catalyst; With thick olefin stream is introduced alkylation, produce one or more alkylated hydrocarbons.

In further embodiment, capable of being combined from specific embodiments feature and from the feature of other embodiment.For example the feature from an embodiment can make up with the feature from any other embodiment.

In further embodiment, use any method, system or heater described herein, carry out the processing of subsurface formations.

In further embodiment, can add additional feature in specific embodiments described herein.

Description of drawings

Benefiting under following detailed description and the situation with reference to the accompanying drawings, advantage of the present invention will become apparent for a person skilled in the art, wherein:

Fig. 1 has provided the schematic diagram of the embodiment of a part of situ heat treatment system that handles hydrocarbon containing formation.

Fig. 2 has described and has handled the schematic diagram that the mixture of being produced by the situ heat treatment method is used the embodiment of system.

Fig. 3 has described and has handled the schematic diagram that the liquid stream of being produced by the situ heat treatment method is used the embodiment of system.

Although the present invention is easy to carry out various improvement and alternative form, its specific embodiments provides by the by way of example in the accompanying drawing, and can describe in detail herein.Accompanying drawing may not be pro rata.Yet, should be appreciated that accompanying drawing and detailed description thereof are not intended to limit the invention to particular forms disclosed, on the contrary, the present invention intends covering spirit of the present invention and interior all improvement, equivalence and the replacement scheme of scope that drops on the claims definition.

The specific embodiment

Following explanation relate generally to is handled the System and method for of the hydrocarbon in the stratum.This stratum be can handle and hydrocarbon product, hydrogen and other products obtained.

Following explanation relate generally to is handled and is used the System and method for of situ heat treatment method by the formation fluid of hydrocarbon containing formation production.Can handle hydrocarbon containing formation obtain hydrocarbon product, hydrogen, methane and other products,

" hydrocarbon " is normally defined the molecule that is mainly formed by carbon and hydrogen atom.Hydrocarbon also can comprise other element, such as but not limited to halogen, metallic element, nitrogen, oxygen and/or sulphur.Hydrocarbon can be but be not limited to kerogen, pitch, pyrobitumen, oil, natural mineral wax and natural rock asphalt.Hydrocarbon can be positioned at intracrustal matrices or adjacent with it.Parent rock can include but not limited to sedimentary rock, sand, silicate, carbonate, kieselguhr and other porous media." hydrocarbon fluid " is the fluid that comprises hydrocarbon.Hydrocarbon fluid can comprise, carries secretly or be entrained in the non-hydrocarbon fluids, and described non-hydrocarbon fluids is hydrogen, nitrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, water and ammonia for example.

" stratum " comprises one or more layers hydrocarbon bearing formation, one or more layers nonhydrocarbon layer, superstratum and/or underlying strata." superstratum " and/or " underlying strata " comprises a class or how inhomogeneous impermeable material.For example superstratum and/or underlying strata can comprise rock, shale, mud stone or wet/tight carbonate.In position in some embodiments of heat treating process, superstratum and/or underlying strata can comprise one deck hydrocarbon bearing formation or multilayer hydrocarbon bearing formation, and described hydrocarbon bearing formation is impermeable relatively and do not have experience to cause temperature in the situ heat treatment process of the remarkable characteristic variations of hydrocarbon bearing formation in superstratum and/or the underlying strata.For example underlying strata can comprise shale or mud stone, but does not allow to heat under the pyrolysis temperature of superstratum during the situ heat treatment method.In some cases, superstratum and/or underlying strata can have some permeability.

" formation fluid " is meant the fluid that is present in the stratum, and can comprise pyrolyzation fluid, synthesis gas, moving fluid, visbreaking fluid and water (steam).Formation fluid can comprise hydrocarbon fluid and non-hydrocarbon fluids." moving fluid " is meant the fluid in the hydrocarbon containing formation that the result as the heat treatment stratum can flow." visbreaking fluid " is meant the fluid that the viscosity as a result as the heat treatment stratum has reduced.

" fluid of being produced " is meant the formation fluid that shifts out from the stratum.

" converted in-situ method " be meant by thermal source heating hydrocarbon containing formation with raise at least partially layer temperature to more than the pyrolysis temperature so that in the stratum, produce the method for pyrolyzation fluid.

" carbon number " is meant intramolecular carbon number.Hydrocarbon fluid can comprise the various hydrocarbon with different carbon numbers.Hydrocarbon fluid can be described by carbon number distribution.Can distribute and/or activity coefficients and relative volatilities carbon number and/or carbon number distribution by real boiling point.

" thermal source " is to provide heat to arrive any system at least a portion stratum by conduction and/or radiant heat transfer substantially.For example thermal source can comprise electric heater, for example insulated electric conductor, elongate member and/or the conductor arranged in conduit.Thermal source also can comprise by in the outside, stratum or internal-combustion fuel generate the system of heat.This system can be the burner of surface combustion burner, downhole gas burner, aphlogistic distributed combustion device and NATURAL DISTRIBUTION.In some embodiments, the heat that can in one or more thermals source, provide or generate by other energy supply.Other energy can directly heat the stratum, perhaps can apply energy to transmitting on the medium, and described transmission medium directly or indirectly heats the stratum.The one or more thermals source that apply heat to the stratum should be understood and the different energy can be used.Therefore, for example for given stratum, some thermal source can be supplied heat by resistance heater, some thermal source can provide heat by burning, and some thermal source can provide heat by one or more other energy (for example chemical reaction, solar energy, wind energy, biological substance or other reproducible energy).Chemical reaction can comprise exothermic reaction (for example oxidation reaction).Thermal source also can comprise provide heat arrive with the heating location adjacent area and/or in its peripheral region the heater of heater well for example.

" heater " is any system or the thermal source that generates heat in well or in the nigh well bore region.Heater can be but be not limited to electric heater, burner, with the burner of material in the stratum or the material reaction that from the stratum, produces and/or their combination.

" situ heat treatment method " is meant that a layer temperature is higher than the method for temperature that causes moving fluid, hydrocarbonaceous material visbreaking and/or pyrolysis to employing thermal source heating hydrocarbon containing formation to raise at least partially, so that produce moving fluid, visbreaking fluid and/or pyrolyzation fluid in the stratum.

Term " wellhole " is meant the hole in the stratum that forms by probing in the stratum or insertion conduit.Wellhole can have circular basically cross section, perhaps is other cross sectional shape.Term as used herein " well " and " opening " can exchange with term " wellhole " and use when the opening that is meant in the stratum.

" pyrolysis " is owing to apply the chemical bond rupture that heat causes.For example pyrolysis can comprise by independent heating compound is changed into one or more other materials.Heat can be transferred on a part of stratum to cause pyrolysis.In some stratum, a part of stratum and/or other material in the stratum can promote pyrolysis by catalytic activity.

" pyrolyzation fluid " or " pyrolysis product " is meant the fluid that produces basically in the process of pyrolysed hydrocarbon.The fluid that produces by pyrolytic reaction can mix with other fluid in the stratum.This mixture will be regarded as pyrolyzation fluid or pyrolysis product." pyrolysis zone " as used herein is meant and reacted or reacted the stratum volume (for example permeable relatively stratum is as tar sand formation) that forms pyrolyzation fluid.

" cracking " be meant involve that organic compound decomposes and molecular recombination with the technology of generation than the greater number molecule that exists at first.In cracking, be accompanied by hydrogen atom transfer generation series reaction between the molecule.For example naphtha can experience heat cracking reaction formation ethene and H ₂

" visbreaking " be meant in heat treatment process in the fluid disentanglement of molecule and/or in heat treatment process big molecular breakdown become less molecule, thereby cause fluid viscosity to descend.

" condensable hydrocarbon " is the hydrocarbon of condensation under 25 ℃ and 1 absolute atmosphere.Condensable hydrocarbon can comprise the mixture of carbon number greater than 4 hydrocarbon." uncondensable hydrocarbon " is uncondensable hydrocarbon under 25 ℃ and 1 absolute atmosphere.Uncondensable hydrocarbon can comprise carbon number less than 5 hydrocarbon.

" obstruction " is meant to hinder and/or suppress one or more compositions and flows by process vessel or conduit.

" alkene " is the molecule that comprises the unsaturated hydrocarbons with one or more non-aromatics carbon-carbon double bonds.

" gasoline hydrocarbon " is meant that boiling range is the hydrocarbon of 32 ℃ (90)-Yue 204 ℃ (400).Gasoline hydrocarbon includes but not limited to gasoline, VB gasoline and the coker gasoline of direct steaming gasoline, naphtha, fluidisation or thermocatalytic cracking.Measure gasoline hydrocarbon content by ASTM method D2887.

" naphtha " is meant that under 0.101MPa boiling Range Distribution Analysis is 38-200 ℃ a hydrocarbon component.Measure naphtha content by the method D5307 of American Society for Testing Materials (ASTM).

" kerosene " is meant that under 0.101MPa boiling Range Distribution Analysis is 204-260 ℃ a hydrocarbon.Measure kerosene content by ASTM method D2887.

" diesel oil " is meant that boiling Range Distribution Analysis is the hydrocarbon of 260-343 ℃ (500-650) under 0.101MPa.Measure diesel oil content by ASTM method D2887.

" VGO " or " vacuum gas oil " is meant that under 0.101MPa boiling Range Distribution Analysis is 343-538 ℃ a hydrocarbon.Measure VGO content by ASTM method D5307.

" upgrading " is meant the quality that improves hydrocarbon.The quality that for example improves heavy hydrocarbon can cause the increase of heavy hydrocarbon API Gravity.

" API Gravity " is meant the API Gravity under 15.5 ℃ (60).Measure API Gravity by ASTM method D6822.

" periodic table " is meant the periodic table by International Union of Pure and Applied Chemistry (IUPAC) in October, 2005 regulation.

" X hurdle metal " or " the multiple metal on X hurdle " are meant one or more metals on X hurdle in the periodic table, and/or one or more compounds of one or more metals on X hurdle in the periodic table, and wherein X is equivalent to the column number (for example 1-12) of periodic table.For example " the 6th hurdle metal " is meant the metal in the 6th hurdle of periodic table, and/or the compound of one or more metals in the 6th hurdle of periodic table.

" X hurdle element " or " the multiple element on X hurdle " are meant one or more elements on X hurdle in the periodic table, and/or one or more compounds of one or more elements on X hurdle in the periodic table, and wherein X is equivalent to the column number (for example 13-18) of periodic table.For example " the 15th hurdle element " is meant the compound of one or more elements on the 15th hurdle in the element on the 15th hurdle in the periodic table and/or the periodic table.

In the application's scope, in the periodic table in the weight of metal, the periodic table in the weight of metallic compound, the periodic table in the weight of element or the periodic table weight of the compound of element all calculate with the weight of metal or the weight of element.For example if every gram catalyzer uses 0.1g MoO ₃, then the weight of molybdenum is the 0.067g/g catalyzer in the catalyzer that is calculated.

" upgrading " is meant the quality that improves hydrocarbon.The quality that for example improves heavy hydrocarbon can cause the increase of the API Gravity of heavy hydrocarbon.

" recycle oil " is meant the mixture of light cycle and heavy recycle stock." light cycle " is meant that the boiling Range Distribution Analysis by fluid catalytic cracking system production is 430 (221 ℃) hydrocarbon to 650 (343 ℃).Measure light cycle content by ASTM method D5307." heavy recycle stock " is meant that the boiling Range Distribution Analysis by fluid catalytic cracking system production is 650 (343 ℃) hydrocarbon to 800 (427 ℃).Measure heavy recycle stock content by ASTM method D5307.

" octane number " is meant with canonical reference fuel and compares, the evaluation representation of the anti-seismic performance of engine fuel.Measure the octane number that calculates by ASTM D6730.

" tiny balloon " is meant when molten component is blown into ball for example by the volatilization organic component hollow shot-like particle that forms at high temperature the thermal process.

" physical stability " is meant that formation fluid does not demonstrate the ability that is separated or flocculates in the transporting fluid process.Measure physical stability by ASTM method D7060.

" chemical stability " is meant that it did not have component reaction to form the polymer of blocking pipeline, valve and/or container and/or the ability of composition when formation fluid betransported.

Fig. 1 has described the schematic diagram of the embodiment of a part of situ heat treatment system that handles hydrocarbon containing formation.The situ heat treatment system can comprise barrier wells 200.Use barrier wells around processing region, to form screen layer.The screen layer suppression fluid flows out and/or the inflow processing region.Barrier wells includes but not limited to dewatering well, vacuum well, capture well, injector well, mud well, freezing well or their combination.In some embodiments, barrier wells 200 is dewatering wells.Dewatering well can be removed liquid water and/or suppress liquid water and enter in a part of stratum to be heated or in the stratum of heating.In the embodiment that Fig. 1 describes, provided the barrier wells 200 of only extending, but barrier wells is typically surrounded whole thermals source 202 of the processing region on heating stratum employed or to be used along a side of thermal source 202.

Thermal source 202 places at least a portion stratum.Thermal source 202 can comprise heater, for example the conductor heater in the insulated electric conductor, conduit, surface combustion burner, aphlogistic distribution/or the burner of NATURAL DISTRIBUTION.Thermal source 202 also can comprise the heater of other type.Thermal source 202 provides heat to arrive at least a portion stratum with the hydrocarbon in the heating stratum.Can be by supply line 204 supplying energies to thermal source 202.Supply line 204 structurally can be different, and this depends on the type of heating employed a kind of thermal source in stratum or multiple thermal source.The supply line 204 that is used for thermal source can transmit the electricity that is used for electric heater, can transport the fuel that is used for burner, perhaps can transport the heat exchanging fluid that circulates in the stratum.

When the heating stratum, the heat that is input in the stratum can cause that expand in the stratum and the geomechanics motion.But the computer simulation simulated formation is to the response of heating.The analog development that can use a computer is used for activating the pattern and the time series of thermal source in the stratum, so that the motion of the geomechanics on stratum can not influence the function of the miscellaneous equipment in thermal source, producing well and the stratum negatively.

The heating stratum can cause that the permeability on stratum and/or porosity increase.Permeability and/or porosity increase can come from the stratum material and reduce, this be because the gasification of water and remove, the removing and/or producing due to the fracture of hydrocarbon.Because the permeability on stratum and/or porosity increase, fluid may flow in the heating part on stratum easilier.Because the permeability and/or the porosity that increase, the fluid in the heating part on stratum can move sizable distance by the stratum.Sizable distance can be to surpass 1000m, and this depends on various factors, for example the temperature on the performance of the permeability on stratum, fluid, stratum and the barometric gradient that allows fluid to move.Advance in the stratum ability of sizable distance of fluid allows producing well 206 to be arranged in the stratum at interval relatively far.

Use producing well 206 from the stratum, to remove formation fluid.In some embodiments, producing well 206 comprises thermal source.Thermal source in producing well can heat at the producing well place or near one or more parts on the stratum it.In some situ heat treatment method embodiments,, be fed to heat in the stratum less than being fed to the heat on stratum from the thermal source on heating stratum in every meter thermal source from producing well in every meter producing well.The heat that is fed to the stratum from producing well can and be removed the liquid phase fluid adjacent with producing well by evaporation, and/or increase the permeability on the stratum adjacent, thereby the permeability on the increase stratum adjacent with producing well with producing well by forming the fracture of macroscopic view and/or microcosmic.

Multiple thermal source can be arranged in the producing well.When the heat stack heating stratum from adjacent thermal source is enough to weaken the producing well heating benefit that the stratum provided, can be closed in the thermal source of producing well bottom.In some embodiments, when the thermal source inactivation of producing well bottom, the thermal source on producing well top can keep work.Can suppress the condensation and the backflow of formation fluid at the thermal source of this aboveground portion.

In some embodiments, the thermal source in producing well 206 allows to remove the gas phase formation fluid from the stratum.Provide at the producing well place or by producing well heat can: (1) when produce fluid with superstratum adjacent production well in when mobile, suppress the condensation and/or the backflow of this production fluid, (2) increase the heat that is input in the stratum, (3) compare with the producing well that does not have thermal source, increase is from the productivity ratio of producing well, (4) suppress higher carbon compounds (C6 and more than) condensation in producing well, and/or (5) are increased in the producing well place or near the permeability on stratum it.

The fluid pressure that subsurface pressure in the stratum can be equivalent to generate in the stratum.When the temperature in the heating part on stratum increases, generate and the result of the gasification of water as the fluid that increases, the pressure in heating part can increase.The control speed that fluid shifts out from the stratum can allow to control the pressure in the stratum.Can be at many diverse locations, for example near producing well place or its, near thermal source place or its, perhaps be determined at pressure in the stratum at monitoring Jing Chu.

In some hydrocarbon containing formations, produce hydrocarbon by the stratum and be suppressed, up at least some hydrocarbon in the stratum by pyrolysis.When formation fluid has the quality of selection, can be by grown place, stratum layer fluid.In some embodiments, the quality of selection comprises the API Gravity at least about 20 °, 30 ° or 40 °.Suppress to produce and to be increased the conversion ratio that heavy hydrocarbon changes into light hydrocarbon by pyrolysis up at least some hydrocarbon.The inhibition initial production can minimize the output from the heavy hydrocarbon on stratum.Producing significantly, a large amount of heavy hydrocarbons can require the equipment of costliness and/or the life-span of reducing production equipment.

In some hydrocarbon containing formations, in the time of can producing significantly big permeability in the heating part on stratum, the hydrocarbon in the heating stratum is to pyrolysis temperature.The FLUID TRANSPORTATION that initial permeability can not suppress completely to be generated is to producing well 206.In initial heating process, the fluid pressure around thermal source 202 in the stratum can increase.Can discharge, monitor, change and/or control the fluid pressure that is increased by one or more thermals source 202.For example thermal source 202 of Xuan Zeing or independent pressure reduction well can comprise dropping valve, and described dropping valve allows to remove some fluids from the stratum.

In some embodiments, can the pressure that pyrolyzation fluid or other fluid produced that allows to generate in the stratum by expanding increases, may not be present in the stratum yet although lead to the open access of producing well 206 or any other diffusing kill-job.Can allow fluid pressure to increase towards lithostatic pressure power.For example in the heating part on stratum, can 206 formation rupture from thermal source 202 to producing well.The generation fracture can discharge some pressure in this part in heating part.Pressure in the stratum may must be kept and be lower than selection pressure suppressing the fracture of undesired production, superstratum or underlying strata, and/or the coking of hydrocarbon in the stratum.

After reaching pyrolysis temperature and allowing from the stratum, to produce, can change the pressure in the stratum, to change and/or to control the composition of the formation fluid of being produced, the percentage of condensable fluid is compared in control with the uncondensable fluid in the formation fluid, and/or controls the API Gravity of the formation fluid of being produced.For example reduce pressure and can cause producing more condensable fluid component.Condensable fluid component can contain the alkene of big percentage.

In some situ heat treatment method embodiments, the pressure that can keep in the stratum is enough high, with the formation fluid of promotion production API Gravity greater than 20 °.Keeping in the stratum pressure that increases can be suppressed in the situ heat treatment process and form sediment.The pressure of keeping increase can quicken production gaseous fluid from the stratum.Gas phase is produced and can be allowed to reduce the size of conveying by the employed collecting duct of fluid of stratum production.The pressure of keeping increase can reduce or need not compress formation fluid in the surface, so that carry fluid to handling in the facility in collecting duct.

Keeping the pressure that increases in the heating part on stratum can allow the quality of production to improve and the low relatively a large amount of hydrocarbon of molecular weight astoundingly.Can keep pressure, have the compound more than the selection carbon number of minimum with the formation fluid of toilet production.It can be maximum 25 selecting carbon number, maximum 20, maximum 12, or maximum 8.The compound of some high carbon numbers can be entrained in the steam in the stratum, and can use steam to shift out from the stratum.Keep compound and/or polycyclic hydrocarbon compounds that the pressure that increases in the stratum can be suppressed at entrainment of high carbon number in the steam.In the significantly long time period, high carbon number compound and/or polycyclic hydrocarbon compounds can be retained in the liquid phase in the stratum.The significant time period can provide the time of abundance for the compound of compound pyrolysis formation than low carbon number.

It is believed that the low-molecular-weight relatively hydrocarbon of generation partly be since in a part of hydrocarbon containing formation hydrogen automatic generation and the reaction due to.The hydrogen that the pressure of for example keeping increase can be forced to generate in pyrolytic process enters in the liquid phase in the stratum.But heat the hydrocarbon generation liquid phase pyrolyzation fluid in the temperature pyrolysis stratum of this part in the pyrolysis temperature range.The liquid phase pyrolyzation fluid component that is generated can comprise two keys and/or free radical.Hydrogen (H in liquid phase ₂) can reduce the two keys in the pyrolyzation fluid that is generated, thus reduce by pyrolyzation fluid polymerization that is generated or the possibility that forms long-chain compound.In addition, H ₂The interior free radical of pyrolyzation fluid that also can neutralize and be generated.Therefore, the H in liquid phase ₂The pyrolyzation fluid that can suppress to be generated react each other and/or with the stratum in the reaction of other compound.

The formation fluid of being produced by producing well 206 can be transported in the treatment facility 210 by collection conduit 208.Also can be by thermal source 202 grown place layer fluid.For example can produce fluid, with the pressure in the control stratum adjacent with thermal source by thermal source 202.The fluid of being produced by thermal source 202 can be transported in the gathering line 208 by pipeline or pipeline, and perhaps the fluid of being produced can be delivered directly in the treatment facility 210 by pipeline or pipeline.Treatment facility 210 can comprise separative element, reaction member, upgrading unit, fuel cell, turbine, reservoir vessel and/or other system and the unit that formation fluid that processing is produced is used.Treatment facility can form transport fuel by at least a portion hydrocarbon that the stratum produces.

In some embodiments, the formation fluid of being produced by the situ heat treatment method is transported to eliminator, and formation fluid is divided into the liquid fluid of one or more in-situ treatment methods and/or the gas stream of one or more situ heat treatment methods.Further treat liquid logistics and gas stream obtain required product.

Heating partially, sub-surface can cause that the mineral structure on stratum changes and form particle.Particle can disperse and/or be partly dissolved in the formation fluid.Particle can comprise the metal on periodic table 1-2 hurdle and 4-13 hurdle and/or the compound of metal (for example aluminium, silicon, magnesium, calcium, potassium, sodium, beryllium, lithium, chromium, manganese, copper, zirconium or the like).In some embodiments, particle comprises tiny balloon.In some embodiments, particle is applied, for example is coated with the hydrocarbon in the formation fluid.In some embodiments, particle comprises zeolite.

The endocorpuscular concentration range of formation fluid can be 1-3000ppm, 50-2000ppm, or 100-1000ppm.The scope of particle size can be the 0.5-200 micron, 5-150 micron, 10-100 micron, or 20-50 micron.

In some embodiments, formation fluid can comprise the distribution of particle.The distribution of particle can be but be not limited to three peaks or multimodal distribution.For example three peaks of particle distribute and can comprise that 1-50ppm is of a size of the particle of 5-10 micron, and 2-2000ppm is of a size of the particle of 50-80 micron and the particle that 1-100ppm is of a size of the 100-200 micron.The bimodal distribution of particle can comprise that 1-60ppm is of a size of the particle of 50-60 micron and the particle that 2-2000ppm is of a size of the 100-200 micron.

In some embodiments, particle contiguously layer fluid and catalysis to form carbon number be maximum 25, maximum compound of 20, maximum 12 or maximum 8.In some embodiments, but zeolite granular assisted oxidation and/or reduction formation fluid, with production method common compound that can not occur in the fluid of being produced of producing common use routine.In the presence of zeolite granular, catalytically layer fluid internal double bond compound reduction of layer fluid and hydrogen contiguously.

In some embodiments, can from the fluid of being produced, remove all or part of particle in the fluid of being produced.Can be centrifugal by using, by washing, by pickling, by filter, by electrostatic precipitation, by froth flotation and/or the separation method that passes through other type except that degranulation.

The formation fluid of being produced by the situ heat treatment method can be transported in the eliminator, and logistics is divided into situ heat treatment method liquid stream and situ heat treatment method gas stream.Further treat liquid logistics and gas stream obtain required product.When using known usually condition treat liquid logistics to produce commercial product, but the negative effect process equipment.For example process equipment can stop up.The example of producing the method for commercial product includes but not limited to alkylation, distillation, catalytic reforming, hydrocracking, hydrotreatment, hydrogenation, hydrodesulfurization, catalytic cracking, delayed coking, gasification or their combination.At " Refining Processes 2000 ", HydrocarbonProcessing, Gulf Publishing Co. discloses the method for producing commercial product among the pp.87-142, and the document is introduced by reference at this.The example of commercial product includes but not limited to diesel oil, gasoline, appropriate hydrocarbon gas, jet fuel, kerosene, naphtha, vacuum gas oil (" VGO ") or their mixture.

Process equipment can be stopped up or fouling by the composition in the situ heat treatment method liquid.The occlusion group compound can include but not limited to hydrocarbon and/or the solid by the production of situ heat treatment method.Can in the process of heating situ heat treatment method liquid, form the composition that causes obstruction.Said composition can adhere on the part of appliance and suppress liquid stream and flow by machining cell.

The solid that causes obstruction can include but not limited to organo-metallic compound, inorganic compound, mineral, mineral compound, tiny balloon, coke, half coal ash (semi-soot) and/or their mixture.The granularity of solid can make conventional filtration can not remove this solid from liquid stream.The hydrocarbon that causes obstruction can include but not limited to contain heteroatomic hydrocarbon, aromatic hydrocarbons, cyclic hydrocarbon, cyclodiene and/or acyclic dienes hydrocarbon.In some embodiments, it is solvable or be insoluble in the situ heat treatment method liquid to be present in the solid that causes obstruction in the situ heat treatment method liquid and/or hydrocarbon part.In some embodiments, before the heating or among, conventional filter liquide logistics is not enough and/or can not remove all or some compositions of clog up process equipment effectively.

In some embodiments, by liquid stream is washed and/or desalination, from liquid stream, remove the occlusion group compound to small part.In some embodiments, by filtering the obstruction that at least a portion liquid stream suppresses process equipment through nanofiltration system.In some embodiments, suppress the obstruction of process equipment by hydrotreatment at least a portion liquid stream.In some embodiments, nanofiltration and the liquid stream of hydrotreatment at least a portion then, removing may clog up process equipment and/or make the composition of process equipment fouling.Can further process the liquid stream of hydrotreatment and/or nanofiltration, produce commercial product.In some embodiments, the good antiscale property additive is joined inhibition process equipment obstruction in the liquid stream.People such as people's such as Mansfield United States Patent (USP) 5648305, Wright 5282957, people such as Miller 5173213, Reid 4840720,4810397 and the Fern of Dvoracek 4551226 in the good antiscale property additive is disclosed, all these at this by with reference to introducing.The example of commercially available additive includes but not limited to that Chimec RO 303, Chimec RO304, Chimec RO305, Chimec RO306, Chimec RO307, Chimec RO308 are (available from Chimec, Rome, Italy), GE-BetzThermal Flow 7R29, GE-Betz ProChem 3F28, Ge-Betz ProChem 3F18 are (available from GE Water and Process Technologies, Trevose, PA, U.S.A.).

Fig. 2 has described the schematic diagram by the embodiment of the system of situ heat treatment method liquid stream and/or situ heat treatment method gas stream production crude oil products and/or commercial product.Formation fluid 212 enters fluid separation element 214 and is divided into situ heat treatment method liquid stream 216, situ heat treatment method gas 218 and aqueous stream 220.In some embodiments, fluid separation element 214 comprises sudden cold-zone.When the formation fluid of being produced enters sudden cold-zone, sudden cold fluid for example water, undrinkable water and/or other component can join in the formation fluid sudden cold and/or the cooling formation fluid to the temperature that is suitable in downstream processing equipment, handling.Sudden cold formation fluid can suppress to promote the compound of the physics of fluid and/or chemical instability to form (for example suppress can precipitation, accelerated corrosion and/or fouling from the solution of upstream device and/or pipeline compound form).Sudden cold fluid can be used as spray and/or the liquid stream form is incorporated in the formation fluid.In some embodiments, formation fluid is incorporated in the sudden cold fluid.In some embodiments, from formation fluid, remove some heats by making formation fluid flow through heat exchanger, thereby cool off this fluid.When the temperature of formation fluid for or when approaching the dew point of sudden cold fluid, sudden cold fluid can be joined in the formation fluid of cooling.Sudden cold formation fluid can improve salt (for example ammonium salt) dissolving that may cause sudden cold fluid chemistry and/or physical instability during under the dew point of sudden cold fluid or near its dew point.In some embodiments, sudden cold in employed water yield minimum so that the salt of inorganic compound and/or other component can not be separated with this mixture.In separative element 214, the sudden cold fluid of at least a portion can be separated with sudden cold mixt, and the cycle of treatment of utilizing minimum is in sudden cold-zone.Can be captured and be used for other facility by the sudden cold heat that produces.In some embodiments, can in sudden cold process, produce steam.The steam that is produced can be transported in the gas separation unit 222 and/or be transported in other facility for processing.

In the heat treating process, gas 218 can enter gas separation unit 222 in position, with divided gas flow hydrocarbon stream 224 from situ heat treatment method gas.In some embodiments, gas separation unit is rectifying absorption and high pressure fractionation unit.Carburet hydrogen logistics 224 comprises carbon number and is at least 3 hydrocarbon.

In the heat treating process, liquid stream 216 enters fluid separation applications unit 226 in position.In some embodiments, fluid separation applications unit 226 not necessarily.In fluid separation applications unit 226, the liquid stream 216 that separates the situ heat treatment method produces carburet hydrogen logistics 228 and saliferous process liquid logistics 230.Carburet hydrogen logistics 228 can comprise carbon number and be 5 hydrocarbon at the most.Part carburet hydrogen logistics 228 can make up with carburet hydrogen logistics 224.Saliferous process liquid logistics 230 can form liquid stream 234 by desalination unit 232 processing.Use known desalination and water-eliminating method, desalination unit 232 is removed mineral salt and/or water from saliferous process liquid logistics 230.In some embodiments, desalination unit 232 is in the upstream of fluid separation applications unit 226.

Liquid stream 234 is at least 5 hydrocarbon including but not limited to carbon number and/or contains heteroatomic hydrocarbon (hydrocarbon that for example contains nitrogen, oxygen, sulphur and phosphorus).Liquid stream 234 can comprise: 0.001g at least, and 0.005g at least, or 0.01g boiling Range Distribution Analysis under 0.101MPa is 95-200 ℃ a hydrocarbon at least; At least 0.01g, 0.005g at least, or 0.001g boiling Range Distribution Analysis under 0.101MPa is 200-300 ℃ a hydrocarbon at least; At least 0.001g, 0.005g at least, or 0.01g boiling Range Distribution Analysis under 0.101MPa is 300-400 ℃ a hydrocarbon at least; At least 0.001g, 0.005g at least, or 0.01g boiling Range Distribution Analysis under 0.101MPa is 400-650 ℃ a hydrocarbon at least.In some embodiments, liquid stream 234 contains the water of maximum 10wt%, the water of maximum 5wt%, the water of 1wt%, or the water of maximum 0.1wt% at most.

After flowing out desalination unit 232, liquid stream 234 enters in the filtration system 236.In some embodiments, filtration system 236 links to each other with the outlet of desalination unit.Filtration system 236 is separated at least a portion and is stopped up compound from liquid stream 234.In some embodiments, the filtration system 236 that is slidingly installed.The filtration system that is slidingly installed 236 can allow filtration system to move on to another from a machining cell.In some embodiments, filtration system 236 comprises one or more membrane separators, for example one or more NF membrane or one or more reverse osmotic membrane.

Film can be ceramic membrane and/or polymer film.Can to be the molecular weight cutoff value be 2000 dalton (Da) at the most, 1000Da or the ceramic membrane of 500Da at most at most to ceramic membrane.Ceramic membrane needn't swelling be removed required material (for example removing the occlusion group compound from liquid stream) so that operate from matrix under optimum condition.In addition, ceramic membrane can at high temperature use.The example of ceramic membrane includes but not limited to middle pore titanium oxide, mesopore gama-alumina, mesopore zirconia, mesoporous silica and their combination.

The bottom (supporting layer) that polymer film comprises the top layer of being made by dense film and made by perforated membrane.The dense film top layer passes through bottom then but arranged polymeric film permission liquid stream (penetrating fluid) is at first flowed through, and fits on the bottom so that the pressure reduction on the film promotes top layer.Polymer film is the organic or hydrophobic film of parent, so that the water that exists in liquid stream is retained or be retained in basically and ooze in the masking liquid.

Compact film can separate at least a portion or all basically occlusion group compounds from liquid stream 234.In some embodiments, by dissolving in its structure with by the diffusion of its structure, the performance of fine and close polymer film makes liquid stream 234 film of flowing through.At least a portion plugging particle may not can dissolve and/or diffuses through dense film, therefore removes them.Plugging particle may not can dissolve and/or diffuses through dense film, and this is because complex structure and/or its molecular weight height of plugging particle.Compact film can be included in the cross-linked structure described in people's such as Schmidt the WO96/27430, the document at this by with reference to introducing.The thickness range of compact film can be 1-15 micron, 2-10 micron or 3-5 micron.

Can make dense film by polysiloxanes, dimethyl silicone polymer, poly-prestox siloxanes, polyimides, aramid, poly-trimethyl silyl propine or their mixture.Can make the porous bottom by the material that the film mechanical strength is provided, and it can be the employed any perforated membrane of ultrafiltration, nanofiltration or inverse osmosis.The example of this material is polyacrylonitrile, polyamidoimide combination titanium dioxide, PEI, polyvinylidene fluoride, polytetrafluoroethylene (PTFE) or their combination.

Separating in the process of occlusion group compound from liquid stream 234, the pressure differential range on the film can be 5-60bar, 10-50bar or 20-40bar.The separation temperature scope can be from the pour point to 100 of liquid stream ℃ ,-20 to about 100 ℃ approximately, 10-90 ℃ or 20-85 ℃.In the continued operation process, the discharge value of penetrating fluid can be the fore flow flux maximum 50%, fore flow flux maximum 70% or fore flow flux maximum 90%.Weight recovery scope at the raw material penetrating fluid can be 50-97wt%, 60-90wt% or 70-80wt%.

Filtration system 236 can comprise one or more membrane separators.Membrane separator can comprise one or more membrane modules.When using two or more membrane separators, they can be arranged according to parallel construction, flow in second membrane separator with the raw material (seepage remaining liquid) of permission from first membrane separator.The example of membrane module includes but not limited to assembly, plate-and-frame module, doughnut and the tubular assembly that spiral twines.In Encyclopedia of Chemical Engineering, 4 ^ThEd., 1995, John Wiley﹠amp; Sons Inc., Vol.16 discloses membrane module among the p158-164.The U.S. Patent No. 5102551 of people's such as for example Boestert WO/2006/040307, Pasternak, Pasternak 5093002, people such as Feimer 5275726, the people such as 5458774 and Finkle of Mannapperuma 5150118 in the example of the assembly that spiral twines is disclosed, all these at this by with reference to introducing.

In some embodiments, when dense film is used for filtration system 236, the assembly that uses spiral to twine.The assembly that spiral twines can comprise that the penetrating fluid dividing plate is clipped in the film assembly of two diaphragms therebetween and described film assembly in three side seals.The 4th side links to each other with the penetrating fluid delivery channel, so that the zone between film is communicated with the catheter interior fluid.Arrange raw material dividing plate (feed spacer) at the top of a film, and reel around the delivery channel of penetrating fluid and to have the assembly of raw material dividing plate, forms the membrane module of columnar basically spiral winding.The thickness of raw material dividing plate can be 0.6mm, 1mm or 3mm at least at least at least, to allow in the assembly that enough film surfactant packages twine to spiral.In some embodiments, the raw material dividing plate is woven raw material dividing plate.In operating process, raw mix can flow through along the raw material dividing plate between the feed side that is clipped in film from an end of the circle tube assembly between the film assembly.Flow through arbitrary diaphragm of part raw mix arrives per-meate side.The gained penetrating fluid flow in the penetrating fluid delivery channel along the penetrating fluid dividing plate.

In some embodiments, the film separation is continuous technology.Liquid stream 234 flows through on film owing to pressure reduction, to obtain filtered liquid logistics 238 (penetrating fluids) and/or circulating fluid logistics 240 (seepage remaining liquid).In some embodiments, filtered liquid logistics 238 can have the composition and/or the granule density of the system of processing obstruction that causes the downstream of reduction.The output that circulating fluid logistics 240 can increase filtered liquid logistics 238 through the continuous circulation of nanofiltration system reach liquid stream 234 initial volume 95%.Under the situation of the feed side of unclean film, the membrane module that circulating fluid logistics 240 can be twined by spiral is circulation at least 10 hours, at least 1 day or at least 1 week continuously.In case finish filtration, then waste stream 242 (seepage remaining liquid) can comprise the composition that may cause obstruction and/or the particle of high concentration.Waste stream 242 outflow filter systems 236 also are transported to other machining cell, for example delayed coking unit and/or gasification unit.

But filtered liquid logistics 238 outflow filter systems 236 also enter one or more technique units.The technique unit of production crude oil products described herein and/or commercial product can be operated under following temperature, pressure, sources of hydrogen flow, liquid stream flow or their combination, perhaps in other cases according to those conditional operations known in the art.Temperature range is about 200-900 ℃, about 300-800 ℃, or about 400-700 ℃.Pressure limit is about 0.1-20MPa, about 1-12MPa, about 4-10MPa or about 6-8MPa.The liquid hourly space velocity degree scope of liquid stream is about 0.1-30h ^-1, about 0.5-25h ^-1, about 1-20h ^-1, about 1.5-15h ^-1, or about 2-10h ^-1

In Fig. 2, filtered liquid logistics 238 and hydrogen source 244 enter hydrotreatment unit 248.In some embodiments, hydrogen source 244 in entering hydrotreatment unit 248 before, can join in the filtered liquid logistics 238.In some embodiments, enough hydrogen is present in the liquid stream 234 and does not need hydrogen source 244.In hydrotreatment unit 248, in the presence of one or more catalyzer, filtered liquid logistics 238 contacts with hydrogen source 244 and produces liquid stream 250.Can operate hydrotreatment unit 248, so that change the liquid stream 250 of all or at least a portion fully, with the composition of removing the equipment that may be blocked in hydrotreatment unit 248 arranged downstream and/or suppress to form this composition.Employed catalyzer can be commercially available catalyzer in hydrotreatment unit 248.In some embodiments, do not need hydrotreatment liquid stream 234.

In some embodiments, in the presence of one or more catalyzer, contact liq logistics 234 and hydrogen to change one or more required performances of crude oil material, are carried and/or the refining specification requirement thereby satisfy.U.S. Patent application 20050133414 in people's such as Bhan announcement, the title that submit to people's such as Wellington 7,20050133405 and 2006 on April is the U.S. Patent Application Serial Number 11/400542 of " Systems; Methods; and Catalysts for Producing aCrude Product ", the title that Bhan submitted on June 6th, 2006 be " Systems; Methods; and Catalysts forProducing a Crude Product " 11/425979, the title of submitting on June 6th, 2006 with people such as Wellington be " Systems; Methods; and Catalysts forProducing a Crude Product " 11/425992 in the method that changes one or more desired properties of crude oil material is disclosed, all these at this by with reference to introducing.

In some embodiments, hydrotreatment unit 248 is to select hydrogenation unit.In hydrotreatment unit 248, select hydrogenation of liquid logistics 234 and/or filtered liquid logistics 238, so that alkadienes is reduced into monoolefine.For example at DN-200 (Criterion Catalysts﹠amp; Technologies, Houston Texas U.S.A.) exists down, under the gross pressure of 100-200 ℃ temperature range and 0.1-40MPa, liquid stream 234 and/or filtered liquid logistics 238 is contacted with hydrogen produce liquid stream 250.With respect to alkadienes in the liquid stream 234 and monoolefine content, liquid stream 250 comprises the alkadienes of reduction amount and the monoolefine of recruitment.In some embodiments, under these conditions, the conversion ratio that alkadienes changes into monoolefine is at least 50%, at least 60%, at least 80% or at least 90%.Liquid stream 250 flows out hydrotreatment unit 248 and enters in one or more machining cells of hydrotreatment unit 248 arranged downstream.Be arranged in hydrotreatment unit 248 downstream units and can comprise distillation unit, catalytic reforming unit, hydrocracking unit, hydrotreatment unit, hydrogenation unit, hydrodesulfurization unit, catalytic cracking unit, delayed coking unit, gasification unit or their combination.

Liquid stream 250 can flow out hydrotreatment unit 248 and enter in the rectification cell 252.Rectification cell 252 produces one or more crude oil products.Rectifying can include but not limited to atmospheric pressure distil process and/or vacuum distillation technology.Crude oil products includes but not limited to C3-C5 hydrocarbon stream 254, naphtha stream 256, kerosene stream 258, diesel stream 262 and tower base stream 264.Tower base stream 264 is generally comprised within boiling Range Distribution Analysis under the 0.101MPa and is at least 340 ℃ hydrocarbon.In some embodiments, tower base stream 264 is vacuum gas oils.In other embodiments, tower base stream comprises boiling Range Distribution Analysis and is at least 537 ℃ hydrocarbon.Gasoline or other commercial product can be sold and/or further be processed into to one or more crude oil products.

In order to improve the purposes of the logistics of being produced by formation fluid, hydrocarbon of producing in rectifying liquid stream process and the appropriate hydrocarbon gas formation capable of being combined of producing in separating technology gas process have the hydrocarbon of higher carbon number.The appropriate hydrocarbon gas logistics of being produced can comprise the acceptable olefin(e) centent of alkylated reaction.

In some embodiments, the liquid stream of hydrotreatment and the logistics (for example distillate and/or naphtha) and situ heat treatment method liquid and/or formation fluid blend of producing, the fluid of production blend by cut.Compare with formation fluid, this blend fluid can have the physical stability and the chemical stability of raising.With respect to formation fluid, the fluid of blend can have the reactive materials (for example alkadienes, other alkene and/or contain oxygen, sulphur and/or nitrogen compound) of reduction amount, thereby improves the chemical stability of blend fluid.With respect to formation fluid, the fluid of blend can reduce asphalt content, thereby improves the physical stability of blend fluid.Compare with formation fluid and/or liquid stream that the situ heat treatment method is produced, the blend fluid may be more alternative raw material.Compare with formation fluid, the fluid of blend can be more suitable for transportation, uses in the chemical process unit and/or use in refinery unit.

In some embodiments, the fluid of producing by oil shale formation by method described herein can with mink cell focus/Tar sands situ heat treatment method (I HTP) fluid blend.Because oil shale liquid is alkane basically, and mink cell focus/Tar sands IHTP fluid is aromatic hydrocarbons basically, so the fluid of this blend demonstrates the stability of raising.In some embodiments, situ heat treatment method fluid can obtain the raw material be suitable for using with the pitch blend in refinery unit.Blend I HTP fluid and/or pitch and the fluid of being produced can improve the chemistry and/or the physical stability of blend product, thereby this blend can transport and/or be assigned in the machining cell.

C by rectification cell 252 productions ₃-C ₅Hydrocarbon stream 254 and appropriate hydrocarbon gas logistics 224 enter in the alkylation 266.In alkylation 266, alkene in appropriate hydrocarbon gas logistics 224 (for example propylene, butylene, amylene or their combination) and C ₃-C ₅Isoparaffin reaction in the hydrocarbon stream 254 produces hydrocarbon stream 268.In some embodiments, the olefin(e) centent in appropriate hydrocarbon gas logistics 224 is acceptable, and does not need the source olefins of adding.Hydrocarbon stream 268 comprises carbon number and is at least 4 hydrocarbon.Carbon number includes but not limited to butane, pentane, hexane, heptane and octane at least 4 hydrocarbon.In some embodiments, the octane number of the hydrocarbon of being produced by alkylation 266 is greater than 70, greater than 80 or greater than 90.In some embodiments, hydrocarbon stream 268 is suitable for without further processing as gasoline.

In some embodiments, but hydrocracking tower base stream 264 is produced naphtha and/or other products.Yet the gained naphtha may need to reform to change octane number, makes product in the commercial gasoline sales that can be used as.Alternatively, can be in cat cracker treating column bottoms stream 264, produce the naphtha and/or the raw material that are used for alkylation.In some embodiments, naphtha stream 256, kerosene stream 258 and diesel stream 262 have unbalanced alkane, alkene and/or aromatic hydrocarbons.These logistics may not have the alkene and/or the aromatic hydrocarbons of the appropriate amount of using in commercial product.Can form boiling Range Distribution Analysis by these logistics of combination at least a portion is 38 ℃ of extremely about 343 ℃ combined stream 266, changes this imbalance.Catalytic cracking combined stream 266 can produce and be suitable for alkene and/or other logistics used in alkylation and/or other machining cell.In some embodiments, hydrocracking naphtha stream 256 is produced alkene.

In Fig. 2, combined stream 266 and enter in the catalytic cracking unit 270 from the tower base stream 264 of rectification cell 252.Under the cracking conditions of control (for example Kong Zhi temperature and pressure), catalytic cracking unit 270 produce additional C3-C5 hydrocarbon stream 254 ', gasoline hydrocarbon logistics 272 and the kerosene stream 258 of adding '.

Additional C ₃-C ₅Hydrocarbon stream 254 ' can be transported in the alkylation 266, with C ₃-C ₅Hydrocarbon stream 254 makes up, and/or makes up with appropriate hydrocarbon gas logistics 224, produces the gasoline that is suitable for selling.In some embodiments, the olefin(e) centent in appropriate hydrocarbon gas logistics 224 is acceptable and does not need the source olefins of adding.

In some embodiments, the amount of the tower base stream of being produced (for example VGO) is too low, so that can't keep the operation of hydrocracking unit or catalytic cracking unit, with the concentration at the gas stream internal olefin of producing by rectification cell and/or catalytic cracking unit (for example by rectification cell among Fig. 2 252 and/or catalytic cracking unit 270) may be too low so that can't keep the operation of alkylation.Can handle the naphtha of from rectification cell, producing, produce alkene for for example further handling in the alkylation.When by the liquid stream of situ heat treatment method liquid production during as feed stream, the reprovision gasoline of the naphtha reforming explained hereafter by routine may not satisfy the commercial formats requirement, for example mandatory provision of California Air Resources Board.Before reformed naphtha technology, in the hydrotreatment process of routine, can make the amount of alkene in the naphtha saturated.Therefore, the reform naphtha of all hydrotreatments can cause being higher than required arene content in the gasoline product (gasoline pool) that is used for reprovision gasoline.Can change in the naphtha internal olefin of reforming and the imbalance of arene content by produce sufficient alkylates by alkylation, to produce reprovision gasoline.The alkene that generates by rectifying and/or pressure naphtha, for example propylene and butylene, can with iso-butane combinations produce gasoline.In addition, find that the naphtha that catalytic cracking is produced in rectification cell and/or other rectifying logistics require the heat that adds, this is because descend with respect to the output of coke for employed other raw material in the catalytic cracking unit.

Fig. 3 has described and has handled the schematic diagram that the liquid stream of being produced by the logistics of situ heat treatment method is produced alkene and/or liquid stream.Disclose the similar approach of producing middle distillate and alkene in people's such as International Publication No. WO 2006/020547 and Mo. U.S. Patent Application Publication Nos.20060191820 and 20060178546, all these are introduced by reference at this.Liquid stream 274 enters catalytic cracking system 278.Liquid stream 274 can include but not limited to liquid stream 250, filtered liquid logistics 238, naphtha stream 256, kerosene stream 258, diesel stream 262 and the tower base stream 264 of liquid stream 234, hydrotreatment from the described system of Fig. 2, any hydrocarbon stream that boiling Range Distribution Analysis is 65-800 ℃ or their mixture.In some embodiments, logistics 276 enters catalytic cracking system 278 and aerosolizable and/or promote liquid stream 274, to strengthen contacting of liquid stream and catalytic cracking catalyst.The steam of atomized liquid logistics 274 can be 0.01-2w/w, perhaps 0.1-1w/w with the scope of the ratio of raw material.

In catalytic cracking system 278, liquid stream 274 is contacted with catalytic cracking catalyst, produce one or more crude oil products.The catalyzer of catalytic cracking comprises the catalytic cracking catalyst of selection, the regeneration Cracking catalyst logistics 280 that at least a portion was used, the Cracking catalyst logistics 282 of at least a portion regeneration or their mixture.Be included in the Cracking catalyst of the regeneration of using in second catalytic cracking system 284 with the regeneration Cracking catalyst of crossing 280.Can use second catalytic cracking system, 284 crackenes to produce alkene and/or other crude oil products.Be provided to hydrocarbon, bio-fuel or their combination that hydrocarbon in second catalytic cracking system 284 can comprise the C3-C5 hydrocarbon produced by producing well, gasoline hydrocarbon, hydrogenation wax (hydrowax), be produced by Fischer-tropsch process.Can improve the output of C3-C5 alkene to the mixture that uses the inhomogeneity hydrocarbon feed in second catalytic cracking system, to satisfy the alkylation demand.Therefore, can improve the integrated of product and refinery practice.Second catalytic cracking system 284 can be known any unit or a structure in the combination of close facies unit, fixing fluid-bed unit, riser, above-mentioned unit or the crackene field.

Catalytic cracking catalyst contacts with liquid stream 274 and will produce crude oil products and useless Cracking catalyst in catalytic cracking system 278.Crude oil products can include but not limited to hydrocarbon, a part of liquid stream 274 or their mixture of boiling point distribution less than the boiling point distribution of liquid stream 274.Crude oil products and useless catalyzer enter piece-rate system 286.Piece-rate system 286 can comprise for example distills unit, stripper, filtration system, centrifuge or any device that can separate crude oil products and dead catalyst known in the art.

The waste cracking catalyst logistics 288 that separates flows out piece-rate system 286 and enters regeneration unit 290.In regeneration unit 290, useless Cracking catalyst contacts under the carbon burning condition with the oxygen source 292 such as oxygen and/or air, produces the Cracking catalyst logistics 282 and the burning gases 294 of regeneration.Can be used as the by-product form of removing the carbon that in the catalytic cracking process process, on catalyzer, forms and/or other impurity and form burning gases.

Temperature range in the regeneration unit 290 can be about 621-760 ℃ or 677-715 ℃.Pressure limit in the regeneration unit 290 can be to be pressed onto 0.345MPa or 0.034-0.345MPa from atmosphere.The time of staying scope of the waste cracking catalyst that separates in regeneration unit 290 is about 1-6 minute, or about 2 minutes, perhaps about 2-4 minute, or about 4 minutes.In the coke content on the Cracking catalyst of regeneration less than the coke content on the waste cracking catalyst that separates.This coke content is less than 0.5wt%, wherein wt percentage with do not comprise coke content the weight of regeneration Cracking catalyst be benchmark.Coke content scope in the Cracking catalyst of regeneration can be 0.01-0.5wt%, 0.05-0.3wt% or 0.1-0.1wt%.

In some embodiments, the Cracking catalyst logistics 282 of regeneration can be divided into two bursts of logistics, the wherein Cracking catalyst logistics 282 of at least a portion regeneration ' leave regeneration unit 290 and enter second catalytic cracking system 284.At least the Cracking catalyst logistics 282 of another part regeneration is left regenerator 290 and is entered in the catalytic cracking system 278.The relative quantity of the regeneration Cracking catalyst that adjusting was used and the Cracking catalyst of regeneration is to provide required cracking conditions in catalytic cracking system 278.Regulate with the regeneration Cracking catalyst of crossing and the ratio of the Cracking catalyst of regeneration and can assist the cracking conditions that is controlled in the catalytic cracking system 278.Weight ratio scope with the Cracking catalyst of regeneration Cracking catalyst of crossing and regeneration can be 0.1: 1 to 100: 1,0.5: 1 to 20: 1 or 1: 1 to 10: 1.For operated system under stable state, approach to be passed to the weight ratio of the regeneration Cracking catalyst of the Cracking catalyst of at least a portion regeneration of second catalytic cracking system 284 and the remainder that the liquid stream 274 interior with being incorporated into catalytic cracking system 278 mixes with the regeneration Cracking catalyst of crossing and the weight ratio of the Cracking catalyst of regeneration, so aforementioned range also can be applicable to this weight ratio.

Crude oil products 296 leaves piece-rate system 286 and enters in the fluid separation applications unit 298.Fluid separation applications unit 298 can be recovery known to those skilled in the art and separate crude oil products become product stream for example gas stream 228 ', any system of gasoline hydrocarbon logistics 300, recycle oil logistics 302 and tower base stream 304.In some embodiments, tower base stream 304 is recycled in the catalytic cracking system 278.Fluid separation applications unit 298 can comprise assembly and/or unit, for example absorber and stripper, rectifier, compressor reducer and eliminator or reclaim any combination with the known system of products of separated from crude oil products.In some embodiments, the recycle oil logistics 302 of at least a portion lightweight is left fluid separation applications unit 298 and is entered in second catalytic cracking system 278.In some embodiments, there is not the light cycle logistics to be transported in second catalytic cracking system.In some embodiments, at least a portion gasoline hydrocarbon logistics 300 is left fluid separation applications unit 298 and is entered in second catalytic cracking system 284.In some embodiments, there is not the gasoline hydrocarbon logistics to be transported in second catalytic cracking system.In some embodiments, gasoline hydrocarbon logistics 300 is suitable for selling and/or using in other technology.

Gasoline hydrocarbon logistics 306 (for example vacuum gas oil) and/or a part of gasoline hydrocarbon logistics 300 and light cycle logistics 302 are transported in the catalytic cracking system 284.Logistics 276 ' in the presence of these logistics of catalytic cracking produce thick olefin stream 308.Rough system logistics 308 can comprise carbon number and be at least 2 hydrocarbon.In some embodiments, thick olefin stream 308 contains the C of 30wt% at least ₂-C ₅The C of alkene, 40wt% ₂-C ₅Alkene, the C of 50wt% at least ₂-C ₅Alkene, the C of 70wt% at least ₂-C ₅Alkene or the C of 90wt% at least ₂-C ₅Alkene.Can in whole process system, provide gas oil hydrocarbon stream 306 to change into C in recycle gasoline hydrocarbon stream 300 to second catalytic cracking systems 284 ₂-C ₅The additional conversion of alkene.

In some embodiments, second catalytic cracking system 284 comprises intermediate reaction district and stripping zone, and the two fluid communication with each other and stripping zone are positioned at below, intermediate reaction district.Compare with its speed in the intermediate reaction district, for high vapor (steam) velocity is provided in stripping zone, the sectional area of stripping zone is less than the sectional area in intermediate reaction district.The sectional area of stripping zone can be 0.1: 1 to 0.9: 1,0.2: 1 to 0.8: 1 or 0.3: 1 to 0.7: 1 with the scope of the ratio of the sectional area in intermediate reaction district.

In some embodiments, the geometry of second catalytic cracking system makes it be generally cylindrical shape, and the draw ratio of stripping zone makes required high vapor (steam) velocity to be provided in stripping zone and to provide in stripping zone carries the regenerated catalyst of using that removes sufficient time of contact from second catalytic cracking system for required ground vapour.Therefore, the draw ratio scope of stripping zone can be 1: 1 to 25: 1,2: 1 to 15: 1 or 3: 1 to 10: 1.

In some embodiments, be independent of the operation or the control of catalytic cracking system 278, operate or control second catalytic cracking system 284.This independent operation or control second catalytic cracking system 284 and can improve gasoline hydrocarbon and change into for example total conversion of ethene, propylene and butylene of required product.Adopt the independent operation of second catalytic cracking system 284, can reduce the cracking level of catalytic cracking unit 278, optimize C ₂-C ₅The productive rate of alkene.Temperature range in second catalytic cracking system 284 can be that 482 ℃ (900 °F) are to about 871 ℃ (1600), 510 ℃ (950)-871 ℃ (1600) or 538 ℃ (1000)-732 ℃ (1350).The operating pressure scope of second catalytic cracking system 284 can be that atmosphere is pressed onto about 0.345MPa (50psig) or about 0.034-0.345MPa (5-50psig).

Join steam 276 in second catalytic cracking system 284 ' can assist the operation control of second catalytic cracking unit.In some embodiments, do not need steam.In some embodiments, with respect to other catalytic cracking process, for gasoline hydrocarbon conversion ratio given in process system and in the gasoline hydrocarbon cracking, use steam that improved C can be provided ₂-C ₅The selectivity of olefins yield wherein increases propylene and butylene productive rate.The scope that is incorporated into steam and the weight ratio of gasoline hydrocarbon in second catalytic cracking system 284 can be to arrive always or be about 15: 1,0.1: 1 to 10: 1,0.2: 1 to 9: 1 or 0.5: 1 to 8: 1.

Thick olefin stream 308 enters in the olefin separation system 310.Olefin separation system 310 can be recovery well known by persons skilled in the art and separate 308 one-tenth C of thick olefin stream ₂-C ₅The olefin product logistics is any system of ethylene product stream 312, propylene product logistics 314 and butylene product logistics 316 for example.Olefin separation system 310 can comprise that system or known the providing from fluid stream 308 such as absorber and stripper, rectifier, compressor reducer and eliminator reclaim and separation of C ₂-C ₅Any combination of the system or equipment of olefin product.In some embodiments, olefin stream 312,314,316 enters alkylation 266 and generates hydrocarbon stream 268.In some embodiments, the octane number of hydrocarbon stream 268 is at least 70, at least 80 or at least 90.In some embodiments, one or more all or part of is transported to other machining cell in the logistics 312,314,316, for example in the polymerized unit, with for use as raw material.

In some embodiments, capable of being combined from catalytic cracking system crude oil products and from the thick olefin stream of second catalytic cracking system.Combined stream can enter in the single separative element (for example combination of liquid separation system 298 and olefin separation system 310).

In Fig. 3, leave second catalytic cracking system 284 and enter in the catalytic cracking system 278 with the Cracking catalyst logistics of crossing 280.Compare with the concentration of carbon on the catalyzer in the Cracking catalyst 282 of regeneration, the catalyzer interior with the Cracking catalyst logistics 280 of mistake can comprise slightly high concentration of carbon.High concentration of carbon can make catalytic cracking catalysed partial inactivation on catalyzer, and described catalytic cracking catalyst provides the olefins yield from the raising of catalytic cracking system 278.With the coke content in the regenerated catalyst of crossing can be 0.1wt% or 0.5wt% at least at least.With the coke content scope in the regenerated catalyst of crossing can be 0.1 to about 1wt% or 0.1-0.6wt%.

But employed catalytic cracking catalyst can be the Cracking catalyst of any fluidisation known in the art in the catalytic cracking system 278 and second catalytic cracking system 284.But the Cracking catalyst of fluidisation can be included in the inorganic refractory oxide matrix or the interior molecular sieve with cracking activity that disperses of adhesive of porous." molecular sieve " is meant can separated atom or any material of molecule based on its size separately.Be suitable for comprising pillared clays, delamination clay and crystal aluminosilicate as the molecular sieve of the component in the Cracking catalyst.In some embodiments, Cracking catalyst comprises crystal aluminosilicate.The example of this alumino-silicate comprises Y zeolite, overstable Y zeolite, X zeolite, zeolite beta, zeolite L, christianite, modenite, faujasite and zeolite omega.In some embodiments, the crystal aluminosilicate that uses in Cracking catalyst is X and/or Y zeolite.The U.S. Patent No. 3130007 of Breck discloses y-type zeolite.

Can be by using hydrogen ion, ammonium ion, multivalent metal cation, the cation, magnesium cation or the calcium cation that for example contain rare earth element, or the composition exchanging zeolite of hydrogen ion, ammonium ion and multivalent metal cation, thereby reduction sodium content, up to it less than about 0.8wt%, preferably less than about 0.5wt% with most preferably less than about 0.3wt%, with Na ₂The O form is calculated, and increases stability and/or acidity as the zeolite of component in the Cracking catalyst.The method of carrying out ion-exchange is well-known in the art.

Before using, the zeolite in the combination Cracking catalyst or the inorganic refractory oxide matrix or the adhesive of other molecular sieve component and porous form finished catalyst.Refractory oxide component in finished catalyst can be one or more mixture and a similar item in silica-alumina, silica, alumina, natural or synthesis of clay, column or delamination clay, these components.In some embodiments, the inorganic refractory oxide matrix comprises for example mixture of kaolin, hectorite, sepiolite and Attagel of silica-alumina and clay.Finished catalyst can contain the zeolite of the 5-40wt% that has an appointment or other molecular sieve and greater than the inorganic refractory oxide of about 20wt%.In some embodiments, finished catalyst can contain zeolite or other molecular sieve, the inorganic refractory oxide of about 10-30wt% and the clay of about 30-70wt% of the 10-35wt% that has an appointment.

Can be by any suitable method known in the art, comprising mixing, grinding, blend or homogenizing, the inorganic refractory oxide component of the crystal aluminosilicate in the assembly catalyze Cracking catalyst or other molecular sieve component and porous or its precursor.The example of spendable precursor includes but not limited to the polyoxy cation of alumina, alumina sol, silicon dioxide gel, zirconia, alumina hydrogel, aluminium and zirconium and the alumina of granulation.In some embodiments, combined zeolite and alumino-silicate gel or colloidal sol or other inorganic refractory oxide component, and spray-drying gained mixture produce the finished catalyst particle that diameter range is generally about 40-80 micron.In some embodiments, zeolite or other molecular sieve can grind or mix, extrude, be ground into then required particle size range in other cases with refractory oxide component or its precursor.The average bulk density of finished catalyst can be about 0.30-0.90g/cm ³And pore volume is about 0.10-0.90cm ³/ g.

In some embodiments, the ZSM-5 additive can be incorporated in the middle cracker in second catalytic cracking system 284.When using the ZSM-5 additive with the Cracking catalyst of selecting in middle cracker, the light alkene for example productive rate of propylene and butylene improves.The amount ranges of ZSM-5 is the maximum 30wt% that are incorporated into the regenerated catalyst weight in second catalytic cracking system 284, maximum 20wt% or maximum 18wt%.The amount ranges that is incorporated into the ZSM-5 additive in second catalytic cracking system 284 can be 1-30wt%, 3-20wt% or the 5-18wt% that is incorporated into the regeneration Cracking catalyst weight in second catalytic cracking system 284.

The ZSM-5 additive is to be selected from the crystal aluminosilicate of intermediate pore size or the molecular sieve additive of zeolite series.The molecular sieve that can be used as the ZSM-5 additive includes but not limited at " Atlas ofZeolite Structure Types ", Eds.W.H.Meier and D.H.Olson, Butterworth-Heineman, the third edition, the mesopore zeolite described in 1992.The aperture of mesopore zeolite is generally about 0.5-0.7nm and comprises for example zeolite of MFI, MFS, MEL, MTW, EUO, MTT, HEU, FER and TON structure types (the IUPAC committee of zeolite name).The non-limiting example of this mesopore zeolite comprises ZSM-5, ZSM-12, ZSM-22, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, silicon zeolite and silicon zeolite 2.In the U.S. Patent No. 3770614 of people's such as Argauer United States Patent (USP) 3702886 and Graven, ZSM-5 has been described, these two pieces of documents at this by with reference to introducing.

ZSM-11 is disclosed in the U.S. Patent No. 3709979 of Chu, ZSM-12 is disclosed in people's such as Rosinski the U.S. Patent No. 3832449, with ZSM-21 and ZSM-38 are disclosed in people's such as Bonacci U.S. Patent No. 3948758, ZSM-23 is disclosed in people's such as Plank U.S. Patent No. 4076842, with ZSM-35 is disclosed in people's such as Plank U.S. Patent No. 4016245, all these at this by with reference to introducing.Other suitable molecular sieve comprises silicoaluminophosphate (SAPO), for example SAPO-4 and the SAPO-11 described in people's such as Lok the U.S. Patent No. 4440871; The silicochromium hydrochlorate; Silicic acid gallium, ferrosilite; Aluminum phosphate (ALPO) is for example at the ALPO-11 described in people's such as Wilson the U.S. Patent No. 4310440; Aluminosilicate titanium (TASO) is for example at the TASO-45 described in people's such as Pellet the U.S. Patent No. 4686029; At the borosilicate described in people's such as Frenken the U.S. Patent No. 4254297; Aluminum phosphate titanium (TAPO) is for example at the TAPO-11 described in people's such as Lok the U.S. Patent No. 4500651; With aluminosilicate iron, all these documents are introduced by reference at this.

It can be one group of zeolite of suitable ZSM-5 additive that people's such as Chester U.S. Patent No. 4368114 (at this by with reference to being introduced into) at length discloses.According to conventional methods, the ZSM-5 additive can keep together with the inorganic oxide matrix component of catalysis inactivation.

In some embodiments, the residue by Fig. 2 and 3 described unit productions can be used as the energy.Gasifiable this residue produces gas, and described gas burned (for example in the turbine internal combustion) and/or be injected in the subsurface formations (for example is injected into the carbon dioxide that is produced in the subsurface formations).In some embodiments, make the residue deasphalting produce pitch.Gasifiable described pitch.

Embodiment

Below listed situ heat treatment liquid stream filtration and produce the non-limiting example of alkene by the liquid stream of situ heat treatment.

The nanofiltration of embodiment 1. situ heat treatment method liquid streams

From the situ heat treatment method, obtain fluid sample (500ml, 398.68g).This fluid sample contains 0.0069g sulphur and 0.0118g nitrogen/g fluid sample.The final boiling point of this fluid sample is that the density of 481 ℃ and fluid sample is 0.8474.Filtering the employed film separation unit of this sample is the P28 of breadboard flat sheet membrane Setup Type, and it is available from CM CelfaMembrantechnik A.G. (Sweden).The dimethyl silicone polymer film (GKSS Forschungszentrum GmbH, Geesthact, Germany) of 2 single micron thickness is used as filter medium.Filtration system is operated under 50 ℃ and the pressure reduction on film is 10bar.At the pressure of permeate side near atmospheric pressure.Collect penetrating fluid and cycle through filtration system with the simulation continuous processing.Protect penetrating fluid with nitrogen curtain, prevent to contact with surrounding air.Also collect seepage remaining liquid for analysis.In filter process, 2kg/m ²The average flow flux of/bar/h do not have can measure from initial discharge value decline.Filtered liquid (298.15g, 74.7% rate of recovery) contains 0.007g sulphur and 0.0124g nitrogen/g filtered liquid; With the density of filtered liquid be 0.8459 and final boiling point be 486 ℃.Seepage remaining liquid (56.46g, the rate of recovery 14.16%) contains 0.0076g sulphur and 0.0158g nitrogen/g seepage remaining liquid; And the density of seepage remaining liquid be 0.8714 and final boiling point be 543 ℃.

Embodiment 2. filters and the fouling of unfiltered situ heat treatment method liquid stream is tested

Not filtering and the fouling behavior of filtered liquid sample of test implementation example 1.Use Alcor thermojunction dirt tester to measure the fouling behavior.Alcor thermojunction dirt tester is the small-sized shell-and-tube heat exchanger of being made by 1018 steels, and it used Norton R222 sand papering before using.In process of the test, the outlet temperature (T of monitoring sample _Out) keep heat exchange temperature (T simultaneously _c) under steady state value.As if fouling taking place and deposited material, then increase of the heat resistance of sample and therefore outlet temperature decline on pipe surface.Outlet temperature decline is measuring of the fouling order of severity after the given time period.Temperature after operating 2 hours descends as the indication of the fouling order of severity.ΔT＝T _out(0)-T _out(2h)。T _{Out (0)}Be defined as maximum (stablizing) outlet temperature that when on-test, obtains, notice at first outlet temperature descend after 2 hours or when outlet temperature is stablized 2 hours, write down T at least _{Out (2h)}

In process of the test each time, fluid sample under about 3ml/min continuously circulation through heat exchanger.The time of staying in the heat exchanger is about 10 seconds.Operating condition is as described below: pressure 40bar, T _SampleBe about 50 ℃, T _cBe that 350 ℃ and test period are 4.41 hours.The Δ T of unfiltered liquid stream sample is 15 ℃, and the Δ T of filtered sample is 0.

This embodiment proves that the liquid stream that nanofiltration is produced by the situ heat treatment method is removed at least a portion occlusion group compound.

Embodiment 3. produces alkene by situ heat treatment method liquid stream

Use laboratory scale pilot test system to experimentize.This pilot test system comprises raw material supply system, catalyst cupport and transfer system, riser reactor, stripper, the product of fluidisation separate and gathering system and regenerator fast.Riser reactor is adiabatic riser, and its internal diameter is that 11-19mm and length are about 3.2m.The riser reactor outlet is communicated with the stripper fluid, and described stripper is operated under the temperature identical with riser reactor outlet stream and its mode provides 100% steam stripping efficiency basically.Regenerator is the employed multisection type cyclic regeneration of a regeneration of spent catalyst device.The flow of dead catalyst with control is fed in the regenerator, and in container, collects the catalyzer of regeneration.In laboratory test process each time, obtain material balance at 30 minutes time intervals place.By using online gas chromatographic analysis composite gas sample, and collect the fluid product sample and analysis is spent the night.Flow by measuring catalyzer and by measuring in the Δ coke on the catalyzer (this is during by this unit of operation under stable state, measure the dead catalyst that obtains in test each time and the coke on the regenerated catalyst sample and obtain), thus the productive rate of coke measured.

The liquid stream that fractionation is produced by the situ heat treatment method, acquisition boiling Range Distribution Analysis are 310-640 ℃ vacuum gas oil (VGO) logistics.Contact VGO logistics and the cat cracker E-Cat that contains the fluidisation of 10%ZSM-5 additive at above-described catalysis system.The riser reactor temperature maintenance is under 593 ℃ (1100 °F).The product of being produced contains 0.1402gC in every gram product ₃Alkene, 0.137gC ₄Alkene, 0.0897gC ₅Alkene, the different C of 0.0152g ₅Alkene, 0.0505g isobutene, 0.0159g ethane, 0.0249g iso-butane, 0.0089g normal butane, 0.0043g pentane, 0.0209g isopentane, 0.2728gC ₆Mixture, the 0.0881g boiling Range Distribution Analysis of the hydrocarbon of hydrocarbon and boiling point maximum 232 ℃ (450) is that hydrocarbon, the 0.0769g boiling Range Distribution Analysis of 232-343 ℃ (450-650) is the hydrocarbon of 343-399 ℃ (650-750) and 0.0386g boiling Range Distribution Analysis hydrocarbon and the 0.0323g coke at least 399 ℃ (750).

This embodiment has proved the method for producing crude oil products, the liquid stream that this method is produced from the logistics of formation fluid separating liquid by rectifying, thus produce boiling point at the crude oil products more than 343 ℃; With the catalytic cracking boiling point at the crude oil products more than 343 ℃, thereby produce one or more additional crude oil products, wherein at least a additional crude oil products is second gas stream.

Embodiment 4. produces alkene by the liquid stream that the situ heat treatment method is produced

The boiling Range Distribution Analysis that the naphtha simulation of using thermal cracking is produced by the situ heat treatment method is 30-182 ℃ liquid stream.In every gram naphtha, naphtha contains 0.186g naphthalene, 0.238g isoparaffin, 0.328g normal paraffin hydrocarbons, 0.029g cycloolefin, 0.046g isoalkene, the positive alkene of 0.064g and 0.109g aromatic hydrocarbons.In above-described catalytic cracking system, contact naphtha stream and the FCC E-Cat with 10%ZSM-5 additive are to produce crude oil products.The riser reactor temperature maintenance is under 593 ℃ (1100 °F).This crude oil products comprises in every gram crude oil products 0.1308g ethene, 0.0139g ethane, 0.0966g C4 alkene, 0.0343gC4 isoalkene, 0.0175g butane, 0.0299g iso-butane, 0.0525gC5 alkene, 0.0309gC5 isoalkene, 0.0442g pentane, 0.0384g isopentane, 0.4943gC ₆Mixture, the 0.0201g boiling Range Distribution Analysis of the hydrocarbon of hydrocarbon and boiling point maximum 232 ℃ (450) is that hydrocarbon, the 0.0029g boiling Range Distribution Analysis of 232-343 ℃ (450-650) is the hydrocarbon of 343-399 ℃ (650-750) and 0.00128g boiling Range Distribution Analysis hydrocarbon and the 0.00128g coke at least 399 ℃ (750).C ₃-C ₅The total amount of alkene is the 0.2799g/g naphtha.

This embodiment has proved the method for producing crude oil products, the liquid stream that this method is produced from the logistics of formation fluid separating liquid by rectifying, thus produce boiling point at the crude oil products more than 343 ℃; With the catalytic cracking boiling point at the crude oil products more than 343 ℃, thereby produce one or more additional crude oil products, wherein at least a additional crude oil products is second gas stream.

Claims (20)

1. produce the method for one or more crude oil products, this method comprises:

By underground situ heat treatment method grown place layer fluid;

Layer fluid is produced liquid stream and gas stream discretely;

Provide partially liq logistics at least to the feed side of the film of filtration system, produce seepage remaining liquid and penetrating fluid, wherein seepage remaining liquid comprises the occlusion group compound; With

One or more processing unit for processing penetrating fluids in the nanofiltration system downstream are to form one or more crude oil products.

2. the process of claim 1 wherein that nanofiltration system is slidingly installed.

3. claim 1 or 2 method, wherein film is NF membrane or one or more reverse osmotic membrane.

4. each method of claim 1-3, wherein film is a ceramic membrane.

5. each method of claim 1-4, wherein film comprises top layer of being made by dense film and the supporting layer of being made by perforated membrane.

6. the method for claim 5, wherein dense film contains polysiloxane.

7. each method of claim 1-6, wherein film is arranged in the assembly that spiral twines.

8. each method of claim 1-7, wherein film contains polysiloxane.

9. each method of claim 1-8, wherein liquid stream contains at the most 10wt% water, 5wt% water, 1wt% water or 0.1wt% water at the most at the most at the most.

10. each method of claim 1-9 wherein is provided to liquid stream continuously film at least 10 hours, one day or at least one week and need not cleans the feed side of the film of described filtration system.

11. each method of claim 1-10, wherein the final boiling point of penetrating fluid is lower than the final boiling point of liquid stream, wherein measures boiling point by ASTM method D5307.

12. each method of claim 1-11, wherein at least one processing unit comprises the hydrotreatment unit.

13. each method of claim 1-12, wherein at least one processing unit comprises the selective hydrogenation unit.

14. each method of claim 1-12, wherein at least one processing unit comprises the hydrotreatment unit, further is included in hydrogen with this method and exists down penetrating fluid contact with one or more catalyzer, to produce suitable the transportation and/or the product of refining application.

15. each method of claim 1-14, wherein the situ heat treatment method comprises with one or more thermals source heating hydrocarbon containing formations.

16. each method of claim 1-15, wherein stratum liquid comprises moving fluid, visbreaking fluid, pyrolyzation fluid or their mixture.

17. each method of claim 1-16 further comprises providing to the small part seepage remaining liquid to delayed coking unit and/or gasification unit.

18. each method of claim 1-17 further comprises one or more crude oil products and other component blend to produce gasoline.

19. make the method for transport fuel, this method comprises one or more crude oil products of the method production of using claim 1-18.

20. transport fuel, it comprises one or more crude oil products of producing by the method for claim 1-19.

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