CN101316983B - 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.Possibly need to change the chemistry and/or the physical property of the hydrocarbon materials in the subsurface formations, from subsurface formations, shift out with being more prone 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 the logistics with the solid particle of the similar flow performance of liquid flow.

The formation fluid that uses the situ heat treatment method from subsurface formations, to obtain can be sold and/or processed produce commercial product.The formation fluid of producing through the situ heat treatment method can have and different performance and/or the compositions of formation fluid that obtains through conventional production method.The formation fluid that uses the situ heat treatment method from subsurface formations, to obtain possibly not satisfy the industrial standard of transportation and/or commercial application.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 present invention provides the method for producing one or more crude oil products, and 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 present invention provides the method for producing alkylated hydrocarbons, and 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; At least the part crude oil products separates into one or more hydrocarbon streams, and wherein at least a hydrocarbon stream is the gasoline hydrocarbon logistics; In second catalytic cracking system, thick olefin stream is produced in catalytic cracking part gasoline hydrocarbon logistics at least through 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 characteristic and from the characteristic of other embodiment.For example the characteristic from an embodiment can make up with the characteristic 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 characteristic in specific embodiments described herein.

Description of drawings

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

Fig. 1 has provided the sketch map of handling a part of situ heat treatment system implementation scheme of hydrocarbon containing formation.

Fig. 2 has described and has handled the mixture produced by the situ heat treatment method sketch map with the system implementation scheme.

Fig. 3 has described and has handled the liquid stream produced by the situ heat treatment method sketch map with the system implementation scheme.

Although the present invention is easy to carry out various improvement and alternative form, its specific embodiments provides through the by way of example in the accompanying drawing, and can describe in detail herein.Accompanying drawing possibly 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 and covers spirit of the present invention and interior all improvement, equivalence and the replacement scheme of scope that drops on the accompanying 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 said 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 one type or more 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 said hydrocarbon bearing formation is impermeable relatively and do not have experience to cause the 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 during the situ heat treatment method is arrived in the superstratum.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 from the stratum, shifts out.

" 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 through carbon number distribution.Can distribute and/or activity coefficients and relative volatilities carbon number and/or carbon number distribution through real boiling point.

" thermal source " is to provide heat to arrive any system at least a portion stratum through conduction and/or radiant heat transfer basically.For example thermal source can comprise electric heater, for example insulated electric conductor, elongate member and/or the conductor in conduit, arranged.Thermal source also can comprise the system that generates heat through or internal-combustion fuel outside on the stratum.This system can be the burner of surface combustion burner, downhole gas burner, aphlogistic distributed combustion device and NATURAL DISTRIBUTION.The heat that in some embodiments, can in one or more thermals source, provide or generate through other energy supply.Other energy can directly heat the stratum, perhaps can apply energy to transmitting on the medium, and said 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 in well, perhaps to generate hot any system or thermal source 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 in the stratum, produce moving fluid, visbreaking fluid and/or pyrolyzation fluid.

Term " wellhole " is meant through the hole in the stratum of in the stratum, drilling or inserting conduit formation.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 through 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 through catalytic activity.

" pyrolyzation fluid " or " pyrolysis product " is meant the fluid that in the process of pyrolysed hydrocarbon, produces basically.The fluid that produces through 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 like tar sand formation) that forms pyrolyzation fluid.

" cracking " be meant involve organic compound decompose with 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 through 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 through ASTM method D2887.

" naphtha " is meant that under 0.101MPa boiling Range Distribution Analysis is 38-200 ℃ a hydrocarbon component.Measure naphtha content through 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 through 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 through 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 through 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 through ASTM method D6822.

" periodic table " is meant the periodic table through 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 element and/or the periodic table on the 15th hurdle in 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, the weight of molybdenum is the 0.067g/g catalyzer in the catalyzer that is then 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 the hydrocarbon of 430 ℉ (221 ℃) to 650 ℉ (343 ℃).Measure light cycle content through ASTM method D5307." heavy recycle stock " is meant that the boiling Range Distribution Analysis by fluid catalytic cracking system production is the hydrocarbon of 650 ℉ (343 ℃) to 800 ℉ (427 ℃).Measure heavy recycle stock content through 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 through ASTM D6730.

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

" 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 through 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 sketch map of handling a part of situ heat treatment system implementation scheme of 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, freeze 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 get in the stratum of perhaps heating in a part of stratum to be heated.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 through 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 in the stratum, circulates.

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 in the stratum, activating the pattern and the time series of thermal source, 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 possibly flow in the heating part on stratum more easily.Because the permeability and/or the porosity that increase, the fluid in the heating part on stratum can move sizable distance through 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.In the stratum, the advance 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 through evaporation; And/or increase the permeability on the stratum adjacent, thereby the permeability on the increase stratum adjacent with producing well with producing well through 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 this thermal source of aboveground.

In some embodiments, the thermal source in producing well 206 allows from the stratum, to remove the gas phase formation fluid.The producing well place or provide through producing well heat can: (1) when produce fluid with superstratum adjacent production well in when moving; Suppress the condensation and/or the backflow of this production fluid; (2) increase is input to the heat in the stratum, and (3) are compared with the producing well that does not have thermal source, increases the productivity ratio from producing well; (4) suppress higher carbon compounds (C6 with 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 in the stratum, generate.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 the 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.Suppress initial production and can minimize 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 in the heating part on stratum, producing significantly big permeability, 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 through one or more thermals source 202.Thermal source of for example selecting 202 or independent pressure reduction well can comprise dropping valve, and said dropping valve allows from the stratum, to remove some fluids.

In some embodiments, can the pressure that pyrolyzation fluid or other fluid produced that allows to generate in the stratum through expanding increases, possibly 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.In heating part, produce fracture and can discharge some pressure in this part.Pressure in the stratum possibly 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 in collecting duct, carry fluid to handling in the facility.

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 number of carbons can be entrained in the steam in the stratum, and can use steam from the stratum, to shift out.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, number of carbons compound and/or polycyclic hydrocarbon compounds can be retained in the liquid phase in the stratum.The significant time period can provide the sufficient time to form the compound than low carbon number for the compound pyrolysis.

According to thinking that generating low-molecular-weight relatively hydrocarbon partly is because in a part of hydrocarbon containing formation due to the automatic generation of hydrogen and the reaction.The hydrogen that the pressure of for example keeping increase can be forced in pyrolytic process, to generate gets 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 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 through 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 through pipeline or pipeline, and the fluid of perhaps being produced can be delivered directly in the treatment facility 210 through 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, and 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, to produce the compound that the conventional production method of common use can not occur usually in the fluid of being produced.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 through using, through washing, through pickling, through filter, through electrostatic precipitation, through 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 instance 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 through reference at this.The instance 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 through 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 from liquid stream, remove this solid.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 compsns of clog up process equipment effectively.

In some embodiments, through liquid stream is washed and/or desalination, part is removed the occlusion group compound from liquid stream at least.In some embodiments, through 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 through hydrotreatment at least a portion liquid stream.In some embodiments, nanofiltration and the liquid stream of hydrotreatment at least a portion then, removing maybe 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 through with reference to introducing.The instance 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 by situ heat treatment method liquid stream and/or situ heat treatment method gas stream and has produced the sketch map of the system implementation scheme of crude oil products and/or commercial product.Formation fluid 212 gets into 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 gets into 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 being suitable for treatment temperature in downstream processing equipment.Sudden cold formation fluid can suppress to promote the compound of physics and/or the chemical instability of fluid to form (for example suppress can deposition, 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 through 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, can sudden cold fluid be joined in the formation fluid of cooling.Sudden cold formation fluid can improve salt (for example ammonium salt) dissolving that possibly 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 in cold the 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 get into 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 gets into 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 through 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 at the upper reaches of fluid separation applications unit 226.

Liquid stream 234 comprises but is not limited to carbon number at least 5 hydrocarbon and/or contain 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 gets 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 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 from liquid stream, removing the occlusion group compound) so that under optimum condition, operate from matrix.In addition, ceramic membrane can at high temperature use.The instance 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 processed by dense film and processed 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 in liquid stream, exists 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, through dissolving in its structure with through 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 maybe not can dissolve and/or diffuses through dense film, therefore removes them.Plugging particle maybe not can dissolve and/or diffuses through dense film, and this is because the complex structure of plugging particle and/or its molecular weight are high.Compact film can be included in the cross-linked structure described in people's such as Schmidt the WO96/27430, the document at this through with reference to introducing.The thickness range of compact film can be 1-15 micron, 2-10 micron or 3-5 micron.

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

From liquid stream 234, separating in the process of occlusion group compound, 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 to 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 instance 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 & Sons Inc., Vol.16 discloses membrane module among the p158-164.The United States Patent(USP) 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 instance of the assembly that spiral twines is disclosed, all these at this through 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 film assembly and said film assembly that the penetrating fluid dividing plate is clipped in two diaphragms therebetween are 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 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 through spiral is circulation at least 10 hours, at least 1 day or at least 1 week continuously.Filter in case accomplish, then waste stream 242 (seepage remaining liquid) can comprise the composition that possibly 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 get into 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 gets into hydrotreatment unit 248 with hydrogen source 244.In some embodiments, hydrogen source 244 in getting into 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 possibly 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.The title of submitting in people's such as the U.S. Patent application 20050133414 of people's such as Bhan announcement, Wellington April 7,20050133405 and 2006 be the U.S. Patent Application Serial Number 11/400542 of " Systems; Methods; and Catalysts for Producing aCrude Product ", title that Bhan submitted on June 6th, 2006 be title that the people such as 11/425979 and Wellington of " Systems; Methods; and Catalysts for Producing a Crude Product " submitted on June 6th, 2006 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 pass through the reference introducing at this.

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 &Technologies; Houston Texas; U.S.A.) exist down; Under the gross pressure of 100-200 ℃ temperature range and 0.1-40MPa, make liquid stream 234 and/or filtered liquid logistics 238 and 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 gets 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 get 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 263.Tower base stream 263 is generally comprised within boiling Range Distribution Analysis under the 0.101MPa and is at least 340 ℃ hydrocarbon.In some embodiments, tower base stream 263 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 sold and/or further be processed into to one or more crude oil products can.

In order to improve the purposes of the logistics of being produced by formation fluid, hydrocarbon of in rectifying liquid stream process, producing and the appropriate hydrocarbon gas formation capable of being combined of in the separating technology gas, producing have the more hydrocarbon of number of carbons.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 possibly be more alternative raw material.Compare with formation fluid, the fluid of blend can be more suitable for transportation, in the chemical process unit, uses and/or in refinery unit, use.

In some embodiments, the fluid of producing by oil shale formation through method described herein can with mink cell focus/Tar sands situ heat treatment method (IHTP) 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 in refinery unit, using with the pitch blend.Blend IHTP 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 gets in the alkylation 266 with appropriate hydrocarbon gas logistics 224.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 the source olefins that need not add.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.The octane number of the hydrocarbon of being produced by alkylation 266 in some embodiments, 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 263 is produced naphtha and/or other products.Yet the gained naphtha possibly 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 263, 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 possibly not have the alkene and/or the aromatic hydrocarbons of the appropriate amount of in commercial product, using.Can form boiling Range Distribution Analysis through these logistics of combination at least a portion is 38 ℃ of extremely about 343 ℃ combined stream 264, changes this imbalance.Catalytic cracking combined stream 264 can produce and be suitable for alkene and/or other logistics in alkylation and/or other machining cell, used.In some embodiments, hydrocracking naphtha stream 256 is produced alkene.

In Fig. 2, in combined stream 264 and the tower base stream 263 entering catalytic cracking units 270 from rectification cell 252.Under the cracking conditions of control (for example control temperature and pressure), catalytic cracking unit 270 produce additional C3-C5 hydrocarbon stream 254 ', gasoline hydrocarbon logistics 272 and additional kerosene stream 258 '.

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 a source olefins acceptable and that need not add.

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) maybe 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 through routine possibly not satisfy the commercial formats requirement, the 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 through 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 sketch map that the liquid stream of being produced by the logistics of situ heat treatment method is produced alkene and/or liquid stream.In people's such as International Publication No. WO 2006/020547 and Mo. U.S. Patent Application Publication Nos.20060191820 and 20060178546, disclose the similar approach of producing middle distillate and alkene, all these pass through with reference to introducing at this.Liquid stream 274 gets into 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 263 of liquid stream 234, hydrotreatment from the said system of Fig. 2, any hydrocarbon stream that boiling Range Distribution Analysis is 65-800 ℃ or their mixture.In some embodiments, logistics 276 gets into catalytic cracking systems 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.The regeneration Cracking catalyst of using 280 is included in the Cracking catalyst of the regeneration of using in second catalytic cracking system 284.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), 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 combination or the crackene field of close facies unit, fixing fluid-bed unit, riser, above-mentioned unit.

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 gets into piece-rate system 286 with useless catalyzer.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 gets into 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 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 in regeneration unit 290, separates 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 get into second catalytic cracking system 284.At least the Cracking catalyst logistics 282 of another part regeneration is left regenerator 290 and is got 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.But the regeneration Cracking catalyst that adjusting was used and the cracking conditions of ratio assist control in catalytic cracking system 278 of the Cracking catalyst of regeneration.The weight ratio scope of the regeneration Cracking catalyst of using and the Cracking catalyst of 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; The regeneration Cracking catalyst of using and the weight ratio of the Cracking catalyst of regeneration approach to be passed to the weight ratio of regeneration Cracking catalyst of Cracking catalyst and the remainder that mixes with liquid streams 274 in being incorporated into catalytic cracking system 278 of at least a portion regeneration of second catalytic cracking system 284, so aforementioned range also can be applicable to this weight ratio.

Crude oil products 296 leaves piece-rate system 286 and gets 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 got 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 got 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 in other technology, using.

Gasoline hydrocarbon logistics 306 (for example vacuum gas oil) and/or a part of gasoline hydrocarbon logistics 300 are transported in the catalytic cracking system 284 with light cycle logistics 302.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 in stripping zone, to provide carries the regenerated catalyst of using that from second catalytic cracking system, removes sufficient time of contact 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 the 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 ℉) 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 controling 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 gets in the olefin separation system 310.Olefin separation system 310 can be recovery well known by persons skilled in the art and 308 one-tenth C of crude 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 gets into 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 get in the single separative element (the for example combination of liquid separation system 298 and olefin separation system 310).

In Fig. 3, the Cracking catalyst logistics of using 280 is left second catalytic cracking system 284 and is got in the catalytic cracking system 278.Compare with the concentration of carbon on the catalyzer in the Cracking catalyst 282 of regeneration, the Cracking catalyst logistics used 280 interior catalyzer can comprise slightly high concentration of carbon.High concentration of carbon can make catalytic cracking catalysed partial inactivation on catalyzer, and said catalytic cracking catalyst provides the olefins yield from the raising of catalytic cracking system 278.Coke content in the regenerated catalyst of using can be 0.1wt% or 0.5wt% at least at least.Coke content scope in the regenerated catalyst of using 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 instance 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 in Cracking catalyst, uses is X and/or Y zeolite.The United States Patent(USP) No. 3130007 of Breck discloses y-type zeolite.

Can pass through with 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 reduce 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 the for example mixture of kaolin, hectorite, sepiolite and Attagel of silica-alumina and clay.Finished catalyst can contain zeolite or other molecular sieve of the 5-40wt% that has an appointment 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 through 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 instance 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, can the ZSM-5 additive be incorporated in the middle cracker in second catalytic cracking system 284.When in middle cracker, using the ZSM-5 additive with the Cracking catalyst of selecting, light alkene is the productive rate raising of propylene and butylene for example.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 the 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 United States Patent(USP) 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 through with reference to introducing.

ZSM-11 is disclosed in the United States Patent(USP) No. 3709979 of Chu; ZSM-12 is disclosed in people's such as Rosinski the United States Patent(USP) No. 3832449; With ZSM-21 and ZSM-38 are disclosed in people's such as Bonacci United States Patent(USP) No. 3948758; In people's such as Plank United States Patent(USP) No. 4076842, disclose in ZSM-23 and the United States Patent(USP) No. 4016245 people such as Plank and disclose ZSM-35, all these are introduced through reference at this.Other suitable molecular sieve comprises silicoaluminophosphate (SAPO), for example SAPO-4 and the SAPO-11 described in people's such as Lok the United States Patent(USP) 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 United States Patent(USP) No. 4310440; Aluminosilicate titanium (TASO) is for example at the TASO-45 described in people's such as Pellet the United States Patent(USP) No. 4686029; At the borosilicate described in people's such as Frenken the United States Patent(USP) No. 4254297; Aluminum phosphate titanium (TAPO) is for example at the TAPO-11 described in people's such as Lok the United States Patent(USP) No. 4500651; With aluminosilicate iron, all these documents are introduced through reference at this.

It can be one group of zeolite of suitable ZSM-5 additive that people's such as Chester United States Patent(USP) No. 4368114 (at this through 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 said gas is burnt (for example in the turbine internal combustion) and/or is injected in the subsurface formations (for example to be injected into the carbon dioxide that is produced in the subsurface formations).In some embodiments, make the residue deasphalting produce pitch.Gasifiable said 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 thick 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 with 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 with final boiling point be 543 ℃.

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

Not 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 is using before with Norton R222 sand papering.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 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 that riser reactor, stripper, the product of raw material supply system, catalyst cupport and transfer system, fast fluidized separate and gathering system and regenerator.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 said stripper under the temperature identical with riser reactor outlet stream, operates 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.Through using online gas chromatographic analysis composite gas sample, and collect the fluid product sample and analysis is spent the night.Flow through measuring catalyzer and through measuring, thereby the productive rate of mensuration coke at the Δ coke on the catalyzer (this through this unit of operation under stable state time, measure the dead catalyst that obtains in test each time and obtain) with the coke on the regenerated catalyst sample.

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 ℉).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 hydrocarbon and the 0.0386g boiling Range Distribution Analysis of 343-399 ℃ (650-750 ℉) 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 through 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 ℉).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 hydrocarbon and the 0.00128g boiling Range Distribution Analysis of 343-399 ℃ (650-750 ℉) 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 through 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 (16)

1. produce the method for hydrocarbon product, this method comprises:

At least the feed side of partially liq logistics (234) to the film of nanofiltration system (236) is provided, produces seepage remaining liquid (242) and penetrating fluid (238), wherein seepage remaining liquid (242) comprises the occlusion group compound; Be characterised in that:

The formation fluid (212) that separation is obtained by the situ heat treatment method is produced liquid stream (234) and gas stream (218), and said formation fluid (212) comprises moving fluid, visbreaking fluid, pyrolyzation fluid or their mixture;

One or more processing unit for processing penetrating fluids (238) in the nanofiltration system downstream are to form one or more crude oil products;

At least one processing unit comprises hydrotreatment unit (248); With

Penetrating fluid (238) is contacted, to produce the product that is fit to transportation and/or refining application with one or more catalyzer.

2. the process of claim 1 wherein that nanofiltration system (236) is slidingly installed.

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

4. claim 1 or 2 method, wherein film is a ceramic membrane.

5. claim 1 or 2 method, wherein film comprises top layer of being processed by dense film and the supporting layer of being processed by perforated membrane.

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

7. claim 1 or 2 method, wherein film is arranged in the assembly that spiral twines.

8. claim 1 or 2 method, wherein film contains polysiloxane.

9. claim 1 or 2 method, wherein liquid stream (234) contains at the most 10wt% water, 5wt% water, 1wt% water or 0.1wt% water at the most at the most at the most.

10. claim 1 or 2 method wherein are provided to film at least 10 hours, one day or at least one week continuously with liquid stream and need not clean the feed side of the film of said filtration system (236).

11. the method for claim 1 or 2, wherein the final boiling point of penetrating fluid (238) is lower than the final boiling point of liquid stream (234), wherein measures boiling point through ASTM method D5307.

12. the method for claim 1 or 2, wherein at least one processing unit comprises the selective hydrogenation unit.

13. the method for claim 1 or 2, wherein the situ heat treatment method comprises with one or more thermal source heating hydrocarbon containing formations.

14. the method for claim 1 or 2 further comprises providing at least part seepage remaining liquid (242) to delayed coking unit and/or gasification unit.

15. the method for claim 1 or 2 further comprises one or more hydrocarbon products and other component blend to produce gasoline.

16. make the method for transport fuel, this method comprises one or more hydrocarbon products that use each method of claim 1-15 to produce.

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