CN1060839C - Method and equipment for treating well stream from offshore oil field - Google Patents
Method and equipment for treating well stream from offshore oil field Download PDFInfo
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- CN1060839C CN1060839C CN96197901A CN96197901A CN1060839C CN 1060839 C CN1060839 C CN 1060839C CN 96197901 A CN96197901 A CN 96197901A CN 96197901 A CN96197901 A CN 96197901A CN 1060839 C CN1060839 C CN 1060839C
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Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B35/00—Vessels or similar floating structures specially adapted for specific purposes and not otherwise provided for
- B63B35/44—Floating buildings, stores, drilling platforms, or workshops, e.g. carrying water-oil separating devices
- B63B35/4413—Floating drilling platforms, e.g. carrying water-oil separating devices
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH DRILLING; MINING
- E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/01—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells specially adapted for obtaining from underwater installations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B35/00—Vessels or similar floating structures specially adapted for specific purposes and not otherwise provided for
- B63B35/44—Floating buildings, stores, drilling platforms, or workshops, e.g. carrying water-oil separating devices
- B63B2035/4473—Floating structures supporting industrial plants, such as factories, refineries, or the like
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B21/00—Tying-up; Shifting, towing, or pushing equipment; Anchoring
- B63B21/50—Anchoring arrangements or methods for special vessels, e.g. for floating drilling platforms or dredgers
- B63B21/507—Anchoring arrangements or methods for special vessels, e.g. for floating drilling platforms or dredgers with mooring turrets
- B63B21/508—Anchoring arrangements or methods for special vessels, e.g. for floating drilling platforms or dredgers with mooring turrets connected to submerged buoy
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B22/00—Buoys
- B63B22/02—Buoys specially adapted for mooring a vessel
- B63B22/021—Buoys specially adapted for mooring a vessel and for transferring fluids, e.g. liquids
- B63B22/023—Buoys specially adapted for mooring a vessel and for transferring fluids, e.g. liquids submerged when not in use
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4062—Geographical aspects, e.g. different process units form a combination process at different geographical locations
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH DRILLING; MINING
- E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/34—Arrangements for separating materials produced by the well
- E21B43/40—Separation associated with re-injection of separated materials
Abstract
A process for treating a well stream produced from an offshore oil field, using a vessel cooperating with an underwater buoy to which both the vessel and the risers from the field are anchored. The well stream is passed to a processing plant on board, wherein water, oil and gas are separated from one another. Separated, stabilized oil is stored in storage tanks, while separated gas is passed to a conversion plant on board, for conversion of the gas to synthetic crude oil and/or wax. Also described is a plant comprising such processing plant and such conversion plant comprising at least a synthesis gas unit and a Fischer-Tropsch unit. The total plant (processing plant and conversion plant) is mounted on skids capable of being secured easily exchangeably to the deck of the vessel. Also described is a conversion plant as mentioned, wherein the Fischer-Tropsch unit comprises at least one slurry bubble column reactor (SBCR reactor) having a reactor zone arranged for containing a slurry consisting of liquid products, finely divided catalyst particles and synthesis gas, which reactor is arranged for internal separation of liquid products from the remaining part of the slurry.
Description
Technical field
The present invention relates to a kind of processing and originate from the method and apparatus of logistics in the well of offshore oilfield.The invention still further relates to a kind of by the Fischer-Tropsch synthetic method with natural gas, particularly association conversion of natural gas be the method for synthetic crude and particularly relate to a kind of floating platform at sea, platform or other device on the method for carrying out.The invention still further relates to a kind of device of implementing this method, this device is installed on the easily changeable balladeur train and particularly is installed on the FPSO floating platform (FPSO=floating production, storage and emptying).
Background of invention
Gather former oil require from offshore oilfield logistics in the well is separated into water, oil and gas.The natural gas that accompanies with the crude oil of being gathered in the logistics in well (being commonly referred to the association natural gas) must be accepted the processing of certain mode after separating.Usually, such processing comprises this gas of burning or again this gas is injected the oil field.But, also can be natural gas transport ashore so that further process.Burning has become a kind of unacceptable gas processing method, because this burning is to waste the hydrocarbon source of reducing gradually and also be air pollution source.The oil field mode of reinjecting that increases cost of crude oil production usually can become unacceptable, and this is because cost of production and the cause that adverse effect may be arranged the crude oil that originates from the oil field.The third method of dealing with problems (that is, as by pipeline natural gas transport to continental rise factory so that further process) will be high cost and unpractiaca method under the situation in some long-range oil field.
By the Fischer-Tropsch synthetic method is conversion of natural gas synthesis gas (CO+H
2) and be the method itself that synthesis gas is converted into synthetic crude known, this method has been disclosed in the comprehensive document, for example referring to G.A. Mil Si " synthesis gas being converted into the situation and the future development of liquid fuel ", fuel rolls up 73 (8), 1243-79 page or leaf (1994).In the later stage eighties, for the natural gas that is transported to from offshore oilfield is on the bank handled (especially in South Africa and Malaysia), people have produced interest to said method again.But to the greatest extent known to the inventor, also do not occur any based on the Fischer-Tropsch synthetic technology and be based upon marine so far as the device on platform, jack-up unit, the FPSO device (FPSO=floating production, storage and emptying) that comprises especially floating oil production platform and oil transportation oil tanker, FSU device (FSU=floating storage device), the semisubmersible platform etc.
Recently, people have known makes oil transportation oil tanker itself be connected with loading buoy under water, and floating platform is lived in the grappling simultaneously of this loading buoy.Loading buoy has under water like this formed the oil-collecting point of a control umbilical that is used for one or more flexible risers and for example draws from the seabed oil extraction system.This floating drum is suitable for promoting and being fixed on the relevant floating platform, is transported to for example oil product induction system of the charge of oil jar on floating platform so that set up one from undersea system.
With this technology is starting point, has occurred the various modified floating platforms that can so change simply at work in recent years:
A) itself be connected to oil transportation oil tanker on the loading buoy under water,
B) be fixedly attached on the loading buoy under water and the oil storage floating platform that has the Unloading Device that is used for emptying at its afterbody simultaneously,
C) the oil recovery floating platform that links to each other with the loading buoy under water that comprises whirligig.
Introduced this floating platform of the cooperation between loading buoy under water based on the hull bottom grappling in NO940352, this loading buoy is made of a whirligig with several pipelines.Near its front end, this floating platform has one and is used to receive receiving the cabin under water and receiving the service well that extends between cabin and the floating platform deck of sub-surface buoy.This sub-surface buoy has external buoyancy parts and a central module, these external buoyancy parts are suitable for entering and releasably being fixed on the floating platform of opening downwards and receive the cabin under water, and this central module is rotatably installed on the external component and is anchored on the seabed and with at least one pipeline road that extends to described floating drum from each producing well always and links to each other.
When this class floating drum was fixed in the reception cabin of floating platform, the external buoyancy parts of floating platform and this floating drum are stable to link to each other and can rotate around the central module of this floating drum, and this central module is anchored on the seabed by suitable anchoring device.So floating drum itself has constituted a rotary body or rotating turret.Under the effect of wind, wave and current, this floating platform is being driven around this rotary body and is being rotated.
This spar structures has many tangible advantages.Because the diameter of this floating drum central module is little, in light weight, thus just make this rotary body promptly the external buoyancy parts of this floating drum correspondingly have minor diameter, therefore little dynamic moment of inertia and rotational resistance are just arranged.Between floating platform and floating drum be connected or uncoupling can be undertaken by the mode of simple and fast, even under the bigger bad weather situation of wave, also be like this.In addition, this floating drum can still be connected with this floating platform under nearly all weather condition.If it is extremely abominable that weather becomes, then can remove this connection fast.
In being suitable for the floating platform that uses with above-mentioned spar structures, reception cabin of Bu Zhiing and well are appropriately positioned as described above in the fore portion of this floating platform as described above.This can rationally and simply rebuild existing floating platform so as with as adapt as this floating drum charge of oil system of charge of oil oil tanker.In addition, receive the cabin under water and the combination of the well that between this reception cabin and floating platform deck, extends can access operation the time high safety and pollute the little system of spillage risk.
As for description more specifically to the floating platform of the spar structures of the above-mentioned type and the above-mentioned type, can be referring to International Patent Application PCT/NO92/00054, PCT/NO92/00055 and PCT/NO92/00056.
In NO922043, described and advantageously reequiped floating drum charge of oil system so that on the oil recovery floating platform, gather the embodiment of offshore oil and gas.Among the described therein embodiment, this system comprises a whirligig, and this whirligig is provided with to such an extent that be convenient to be reduced to shaft bottom end operating position or from then on rises on the operating position and it is linking to each other with pipe-line system on the floating platform on the operating position.This whirligig comprise inside and outside can counterrotating rotary part.Be provided with in the upper end of this floating drum one all carry linkage that pipe end all is attached thereto or joint and this linkage to be suitable for respectively being connected and uncoupling with corresponding linkage in this whirligig bottom.
In a preferred embodiment of this system, this whirligig is placed on the lifting gear, and lifting gear is slidably mounted on the track-type facilities, and described track-type facilities extends between aboveground end and downhole end.This whirligig is on its joint or the tram in the linkage connection cabin that can be placed on downhole end simply.As the parts of most critical, this rotation and linkage can keep in repair and change at an easy rate.Can utilize and realize in single stepping at the self-closing valve on these linkage both sides and being connected and uncoupling of the carrier pipe of this floating drum.This whirligig can be easily by the flexible pipe absorption connection and vertical the moving in the uncoupling process, and this flexible pipe is fixed with the well of this whirligig with becoming an angle of 90 degrees.
The major advantage of this system provides the system of Lin Jixiao, and this is because used the special floating drum of a rotary body of formation own.This makes weight saving and device volume reduce, thereby has reduced cost significantly.
Such system will need to reconstruct slightly the oil transportation oil tanker, so that oil is transported on the oil recovery floating platform, the oil tanker of described reconstruction is applicable to above-mentioned floating drum charge of oil system.Except from marginal oil field recovers the oil continuously, with the test of also can periodically working and recover the oil of such oil recovery floating platform.In summer months, this floating platform can the oil transportation oil tanker may have more than needed during in be used for recovering the oil as test.
Since the hand chamber, cabin of this floating platform and its engine room in the fore portion of this floating platform and this floating platform receive the cabin above service well be positioned at back, hand chamber, cabin just, so service well will be positioned at the leeward side of hand chamber, cabin.Under the situation of this layout,, also obtained from this hand chamber, cabin rear backward until the broad deck area in this quarter-deck district except the crewman in this vertical shaft district work is provided the protection.When this floating platform is used as the oil recovery floating platform, this zone will can be used in essential treating apparatus and control well device.
Because floating platform can move about between different movable oil fields, so package unit preferably is divided into portable small-sized parts.
Aforesaid floating platform will be suitable as the mother ship carrier of association conversion of natural gas for the device of for example synthetic crude and/or wax very much.In addition, such arrangement will produce the advantage of being brought by this whirligig system, and this whirligig system is suitable for being used with the operation of water filling, water purifying plant, well water filling etc., and this allows high flexible ground to use floating platform.This system also is applicable to the waters with drift about ice and iceberg, because when needs, it is uncoupling and do not destroy the danger of sub-surface buoy fast.
As top the introduction, the inventor does not know any offshore installation based on the Fischer-Tropsch synthetic technology.But, by the agency of be used to be installed on floating platform, offshore platform and other offshore installation, be the assembly type conversion of natural gas device or the system of synthetic crude with association natural gas or long-range conversion of natural gas, see that in SECONS 1994 (North Sea strategy with economic)-London, the Dr. on the 1994.11.28-29 wears dimension D.J. An Teer and Dr. pauses willing. plucked instrument pause " by with marine conversion of natural gas be the mode of crude oil catch reduce cost and value-added opportunity ".
In the middle of above-mentioned publication, introduced assembly type conversion of natural gas device or system, it can be connected in the new or existing offshore oil production system.It is synthetic crude, wax or methyl alcohol that this assembly type device is used for conversion of natural gas.The disclosure thing is especially at the field devices of the association natural gas that will be used to produce 5-50 MMCF/D (0.14-1.42 hundred cubic meters per day).In this article, determined two class devices:
(a) be designed for the device of before oil field that natural gas is reinjected, from natural gas, removing useful component,
(b) be designed for by conversion of natural gas is processed the device of this natural gas fully for the mode of easy to handle more and valuable product, thereby avoid burning, the oil field or transport natural gas of reinjecting.
In these two kinds of devices, this method comprises two main steps: (1) the synthesis gas of conversion of natural gas for being made of carbon monoxide, hydrogen and carbon dioxide, (2) are converted into synthetic crude to synthesis gas in Fischer-Tropsch synthesis device (FT reactor) in the partial oxidation device.It is said, this method be a kind of allow when operation, be converted into the flexible way that comprises other finished product from light-duty condensate to microwax.
Can arrange two devices that step is used of this method by stowage of sledge independently or cabin group's mode.It is believed that described device is installed on the basis in cabin can guarantee flexibility, this especially is reflected in the device productivity that can improve or reduce this device productivity as required or turn round when producing also liquid storage, the air-flow of different products such as synthetic crude, wax and methyl alcohol.
In order in the first step of this method, from natural gas, to make synthesis gas, in the disclosed article of people such as An Teer, describe several method in detail, wherein importantly partial oxidation, steam reformation, self-heating catalytic reforming and mixing reforming.Consider preferred method for partical oxidation from flexibility, device size, productivity ratio, logicality and economy aspect that efficient, cost, the product of process are formed.
In order to produce synthetic crude and/or wax in second step of this method is that FT is synthetic, can use many dissimilar reactors, promptly the MTFB reactor-it is multitube fixed bed reactors (MTEB=" multitube fixed bed "), fluidized-bed reactor, ring-like bed bioreactor, mortar reactor and Lin De isothermal reactor.In these reactors, the preferred MTFB reactor of people such as An Teer, this is because facts have proved that this reactor cost is low and strong because of operating flexibility in very wide temperature range.This piece publication is claimed: although studied the mortar reactor widely, it also be not proved to be industrial be effective.
The FT reactor uses iron, cobalt or ruthenium catalyst.All these catalyst types allegedly can both be made its composition and comprise from light-duty condensate to heavy paraffin hydrocarbon oil or the product of microwax or paraffins.
So, although there are a lot of bases to show, is the association conversion of natural gas that valuable and more tractable product is reasonable economically and the association natural gas processing mode little to ambient influnence, but still needs a kind of improvement project to realize safer and more favourable operation.
Tying down of the shortcoming that the MT reconnaissance FB reactor of being thought to be used for the preferred reactor of FT synthetic method by people such as An Teer is not subjected at all is big because of its weight, expense is high and design complexity and operating temperature range are narrow.In order to make the pressure drop of passing MTFB reactor catalyst bed in acceptable degree, must use oarse-grained catalyzer, this has brought the restriction of diffusion aspect.So and owing to be difficult to control the temperature of reactor, the conversion per pass of synthesis gas is lower than the conversion ratio that meets the requirements.In addition, under such reactor situation, catalyzer displacement complexity and this reactor are unsuitable for very active catalyzer.
Goal of the invention
At above-mentioned background, an object of the present invention is to provide the method and apparatus of on the floating platform ship, handling logistics in the well that originates from offshore oilfield, described method and apparatus has used the floating platform of working with sub-surface buoy, this floating platform and all be anchored on the sub-surface buoy from the standpipe in oil field.
Another object of the present invention provides natural gas, especially be the method for synthetic crude and/or wax with the association conversion of natural gas, this method is applicable to occasion such as floating platform on sea, platform or other device that the space is limited.
Another object of the present invention provide a kind of simple, compact and operation reliably, be the device of synthetic crude and/or wax with conversion of natural gas.More particularly, the purpose of this invention is to provide a kind of like this association conversion of natural gas device, it is installed on the easy balladeur train that is fixed on floating platform, offshore platform or other offshore installation, particularly the FPSO floating platform (FPSO=" floating production, storage and emptying ") with changing.
A further object of the present invention provides a kind of device of the above-mentioned type, can adjust this device more at an easy rate so that produce the productivity that has the product of different size and also can adjust it at an easy rate.
Summary of the invention
According to a first aspect of the invention, a kind of method of handling logistics in the well that originates from offshore oilfield on the floating platform ship is provided, this method has been used the floating platform of operating with sub-surface buoy, this floating platform and all be anchored on the sub-surface buoy from the standpipe in oil field, whirligig is arranged on the floating platform of floating drum top.The method is characterized in that following step: logistics in the well is fed in the treating apparatus, this treating apparatus is installed on the easy balladeur train that is fixed on the floating platform deck with changing, and described balladeur train is installed on the either side that longitudinally is centrally disposed at the pipe support on the floating platform; In said treating apparatus, make water, oil, natural gas separated from one another; In the storage tank of some floating platform at least, store isolated stabilize oil; Is one of isolated natural gas input the device of synthetic crude and/or wax with this conversion of natural gas, then this synthetic crude and/or wax is stored in the storage tank of floating platform, and this synthetic crude can be mixed arbitrarily with stabilize oil.
According to a second aspect of the invention, provide the device of logistics in the well that a kind of processing originates from offshore oilfield, the layout of this device is suitable for being installed on the floating platform ship and it comprises a treating apparatus, makes water, oil, natural gas separated from one another in this treating apparatus.This device is characterised in that: it comprises that also one is the device of synthetic crude and/or wax with isolated conversion of natural gas, said reforming unit comprises at least one synthesis gas device and a Fischer-Tropsch synthesizer, and package unit (treating apparatus and reforming unit) is installed on the easy balladeur train that is fixed on this floating platform deck with changing.
According to another aspect of the present invention, provide a kind of particularly at sea floating platform, platform or other device go up implement, natural gas, particularly two steps of association natural gas are converted into the method for synthetic crude and/or wax, wherein (1) is this conversion of natural gas the synthesis gas of being made up of the mixture of carbon monoxide, hydrogen and carbon dioxide in the synthesis gas device, and (2) are converted into synthesis gas synthetic crude and/or wax in the Fischer-Tropsch synthesizer.The method is characterized in that: will be in order to implement the reaction zone of the synthetic and synthesis gas that obtain by step (1) of Fischer-Tropsch with a kind of form injection mortar bubble-column reactor (SBCR reactor) of the mortar of forming by liquid form product, segmentation catalyst granules and synthesis gas, liquid form product is isolated in inside from the remainder of mortar in this reactor.
In a preferred embodiment of this method, synthesis gas that cooling is obtained by step (1) and the reaction zone that is injected into the mortar bubble-column reactor after dehydration bottom, said reaction zone are arranged to be used to hold the mortar of being made up of liquid form product, segmentation catalyst granules and the synthesis gas of being supplied with and be used to be contained in the top mutually gas of this mortar; By a fillter section that comprises shell and filtration members liquid form product is separated from the remainder of mortar, described shell and filtration members constitute a filtering area with filtrate product outlet, and said filtration members is arranged to contact with mortar in the reaction zone; At filtering area be included in this mortar gas above mutually and between interior reaction zone part, set up the fluid flow relation; The even pressure reduction of filtration members is passed in formation.
According to another aspect of the present invention, provide a kind of with natural gas, particularly association natural gas two step be converted into synthetic crude and/device of wax, wherein (1) is this conversion of natural gas the synthesis gas of being made up of the mixture of carbon monoxide, hydrogen and carbon dioxide in the synthesis gas device, and (2) will be converted into synthetic crude and/or wax by the synthesis gas that this device obtains in the Fischer-Tropsch synthesizer.This device is characterised in that: this Fischer-Tropsch synthesizer comprises one or more mortar bubble-column reactors (SBCR reactor), each reactor comprises a reaction zone, and described reaction zone is arranged to be used to hold the mortar of being made up of liquid form product, segmentation catalyst granules and synthesis gas; Liquid form product is isolated in the remainder inside that described reactor is arranged to be used for from mortar.
In a preferred embodiment, this device is characterised in that each mortar bubble-column reactor comprises: one constitute one be arranged to be used to hold mortar mutually with container at the reaction zone of the gas of mortar above mutually; In this container bottom this synthesis gas is injected mortar device mutually; Be arranged to fillter section that liquid form product and mortar are separated, this fillter section comprises a shell and the filtration members to small part around this container, this filtration members and said shell constitute a filtering area with filtrate product outlet, and said filtration members is arranged to contact with mortar in the mortar district; At filtering area with form the device of fluid flow between in use by the reaction zone part that is occupied at the gas of mortar above mutually; The device of the even pressure reduction of filtration members is passed in formation.
In a preferred embodiment, this device is installed on the slide rail that can be easy to be fixed on floating platform, offshore platform or other offshore installation, particularly FPSO floating platform (FPSO=" floating production, storage and emptying ") with changing.
Brief description of drawings
Fig. 1 is the simplified flow chart of the inventive method embodiment.
Fig. 2 is the longitudinal sectional view that is used for the mortar bubble-column reactor of FT synthesizer in the methods of the invention.
Fig. 3 is that phantom drawing cuts open in a kind of office with loading oil recovery floating platform of floating drum Load System that is used to load hydro carbons and the space that the device of implementing the inventive method is installed.
Fig. 4 is the phantom drawing with oil recovery floating platform of installation assembly type device of the present invention aboard ship.
Detailed description of the present invention
With reference now to accompanying drawing 1 describe of the present invention be used for natural gas, particularly association conversion of natural gas be synthetic crude and/principal character of the two-stage process of wax and the preferred embodiment of device.Association natural gas under about 40 bar pressures is heated to about 400 ℃ and be injected into absorption tower 1, wherein only with H
2The sulphur that the S form exists is adsorbed in the ZnO grain bed.The processed gas that comes out from the absorption tower mixes with water vapour and this gaseous mixture is heated to about 500 ℃ and injection self-heating recapitalization tower 2.Make the oxygen and mixed being incorporated in of water vapour of from air, extracting inject the self-heating recapitalization tower under about 300 ℃.Also also inject the self-heating recapitalization tower be heated to about 300 ℃ by the synthetic circulating air of FT.The self-heating recapitalization tower comprises that burner that a reactant mixes therein, hydrocarbon and oxygen burn therein and generates the combustion zone of CO and water, remaining hydrocarbon and water and is converted into CO and H therein
2Hot-zone and a follow-up catalyzer loading area, in this loading area, set up on the one hand the balance between CO and the water, set up CO on the other hand
2And H
2Between balance (water-gas shift reaction).Adjust ratio and other reaction condition between reactant, so that at 1.6: 1～2.0: 1 H of the exit of self-heating recapitalization tower 2 acquisition
2: the CO mol ratio.
By water directly being injected in the gas and the synthesis gas Quench to 300 that reclaims by the self-heating recapitalization tower ℃.In heat interchanger, further cool off this synthesis gas and the (not shown) that therefrom dewaters.Then, under about 200 ℃ this synthesis gas is injected the FT synthesizer, in device as shown in the figure, the FT synthesizer is made of two reactors 3.In exothermic process, the component of this synthesis gas reacts to each other and generates hydrocarbon and water.The FT reactor is that (" mortar bubble-column reactor "=SBCR) also uses with the cobalt-base catalyst of alumina as carrier mortar bubble-column reactor type.The three-phase mixture of the gas of forming at this used term " mortar " refers to solid catalyst particle, the synthetic product that obtains is formed by FT liquid hydrocarbon, by unreacted reactant and the gaseous hydrocarbon that in FT synthesizes, forms.
Utilize with the interchange of heat of the water that circulates by the heat-exchange tube that is installed in this SBCR reactor 3 and remove unnecessary heat.Under reaction condition (comprising about 230 ℃), hydrocarbon can exist with gas phase and liquid form.From unreacted synthesis gas of the recovered overhead of reactor 3 and gaseous state hydrocarbon products.The filter that is installed in reactor top is isolated catalyzer from liquid form product.
The gaseous products (not shown) of cooling reactor 3 also is injected in the separator 4, thus the liquid stream that separates water outlet and form by the synthetic crude product that meets the requirements.The water that a part is separated is sent back to the inlet of reformation tower 2.The part of the uncondensed gas that reclaims from separator 4 is sent back to the inlet of reformation tower 2, and the remainder of gas can be used as heating and enters the combustion gas of the raw material in the self-heating recapitalization tower and/or be used for generator for electricity generation or be used for desalinization handling.In order to inject purpose, also can use a part of condensed gas.
Two SBCR reactors shown in the figure are connected, but they also can be in parallel, represents this parallel-connection structure with perforation line in the drawings.When this reactor series connection, can from logistics, remove reaction water and liquid hydrocarbon (C by rights in first reactor downstream
5+), so that improve the efficient of second reactor.If necessary, each reactor 3 that can turn round respectively.
Any catalyzer of the Fischer-Tropsch synthesis mode of producing synthetic crude and/or wax that is applicable to all can be used for the SBCR reactor of apparatus of the present invention, a kind of in for example previously known iron, cobalt, nickel or the ruthenium that this purposes arranged.Preferred catalyzer is to be the cobalt-rhenium catalyst of carrier with the alumina.Can select for use the metal in the rare earth metal family to improve catalyzer arbitrarily.For example, can use with γ-Al
2O
3Cobalt-rhenium catalyst for the Re of the Co that contains 20% (percentage by weight) of base and 1%.Such catalyzer is disclosed among the US4801573, can be according to early stage humidity method Co (NO
3)
26H
2O and HReO
4Aqueous solution dipping γ-Al
2O
3The preparation catalyzer.
Use preferred FT catalyzer, people obtain greater than 85% one way CO conversion ratio (reaching as high as 98%) with greater than 88% C
5+The polymerization probability α of selectivity and 0.9-0.95 according to Anderson-Shu Erci-Fu Luoli distribution.
Preferred catalyzer has caused C with combining of described SBCR reactor
5+Selectivity is strong, CO conversion per pass height, activity of such catalysts and regenerability are stable.
In the method for self-heating recapitalization as be used in the method for above-mentioned apparatus of the present invention the scheme that has adopted partial oxidation to combine with the adiabatic steam-reforming technology.Under the outlet temperature of reactor, gaseous products is in the chemical balance, and outlet temperature is by inlet temperature and thermal insulation warming decision.In fixed bed reactors, implement this method.It is a kind of flexible reforming method that can produce the synthesis gas that its composition changes with the adjustment of operating condition that self-heating recapitalization needs less device and it than conventional steam reformation.
In order from the natural gas of importing this device, to make synthesis gas, even can use other embodiment of reforming method, for example steam reformation, steam reformation and the mixing reforming of self-heating recapitalization combination thereafter, the mixing reforming that has pre-reforming, partial oxidation, the gas heated reformate that combines by self-heating recapitalization and steam reformation thereafter.Other selection can be self-heating recapitalization or the reformation in section's glug reformation tower-heat-exchange system that mixes.
Mortar bubble-column reactor (SBCR)
At the three-phase system reactor that is used for continental rise Fischer-Tropsch synthesizer, what need carry is mechanical agitation type mortar reactor and ring-shaped sand slurry bubble-column reactor.These two kinds of reactors have all utilized the catalyst particles that is dispersed in the liquid.Therefore, under most of occasions, this liquid must separate with mortar so that remove liquid form product or in order to carry out catalyst regeneration.
The operation of mortar bubble-column reactor is very simple, and this is because saved mechanical driving member.Therefore, because low diffusional resistance and effectively heat transmission, these reactors are very attractive to a lot of commercial runs.But Separation of Solid and Liquid is normally outside reactor and finish in the filtration of complexity and settler.This catalyzer mortar will be recovered in the reactor, will use mortar pump sometimes.Therefore, in the continued operation of mortar bubble-column reactor, may run into serious problem.
Discussed the problem that catalyst/wax is separated in Fischer-Tropsch mortar reactor assembly by the report that USDOE delivers recently.This report draws to draw a conclusion: when the internal ramp in being immersed in the reactor mortar was used for some laboratory scale device or medium-sized experimental facilities, this strainer was worked unsuccessful because of operating difficulties.Its part wall is used for medium-sized experimental facilities as the reactor of strainer, but it can not be used for industrial reactor.The danger that internal ramp is subject to stop up, this may cause too early termination work, does not therefore allow to be used for industrial equipment.
This report is also claimed: used the internal ramp in the reactor mortar in research approach.But, though when beginning because of utilizing pressure reduction may make filtrate flows, but strainer just be plugged at once, thereby the conclusion that draws is: continued operation is to realize, thereby, need outside reactor, finish solid/liquid separation for plant-scale running.
Yet, by that the applicant finished, that especially in International Patent Application PCT/NO94/00023, introduced, the recent research of mortar bubble-column reactor is shown: with the front instruction on the contrary, a kind of synthetic continuous reaction apparatus of Fischer-Tropsch that is used for can be provided, wherein not need the sufficiently high filtrate flow velocity that carries out solid/liquid separation in the filter externally and can obtain to be applicable to industrial operation.
The mortar bubble-column reactor that is used for the synthetic continuous reaction system of Fischer-Tropsch is applicable to device of the present invention very much, this reactor is so a kind of reactor, be liquid form product in reactor with contain the mortar that segments the catalyzer in liquid medium and be separated, said reactor comprises: one constituted one be arranged to be suitable for holding mortar mutually with at the mortar container of the reaction zone of the gas on top mutually; Mortar device is mutually injected with this synthesis gas in bottom at this container; Layout is used for fillter section that liquid form product and mortar are separated, this fillter section comprises a shell and the filtration members to small part around this container, filtration members and said shell have constituted a filtering area with filtrate product outlet, and described filtration members is arranged to contact with mortar in the mortar district; At filtering area with set up the device of fluid flow relation between in use by the reaction zone part that is occupied at the gas of mortar above mutually; The device of the even pressure reduction of filtration members is passed in formation.
Have been found that the filtering area and the circulation between the reaction zone that obtain by the above-mentioned design to reactor have prevented to produce solid matter on filtration members.Its mechanism is as follows: the turbulent motion of mortar is upward through fluctuation or the instability that mortar causes the pressure on filtration members because of bubble.Circulation between reaction zone and the filtering area has promoted or has strengthened the fluctuation or the instability of described pressure.Therefore, a kind of like this system is fairly simple and effective.Generally being considered to problematic especially separating step is to implement under the situation of less complex.Under suitable operating condition, filtration members is carried out self cleaning.
Compare with the MTFB reactor, the major advantage of using such SBCR reactor to obtain is especially as follows:
-can improve the thermal control that heat release FT is reacted by using with the incorporate effective heat interchanger of reactor.Improving above-mentioned thermal control makes catalyzer and reactor that high productivity ratio all be arranged.
-this reactor is compact and simple, in the reactor parts seldom, its installation cost is than the low 50-70% of installation cost of fixed bed reactors (MTFB reactor).
-finishing catalyzer separates with the inside of FT product, does not therefore need external discrete catalyzer device.
-because catalyzer is suspended in the mortar in reactor, so can replace catalyzer in operation continuously.
-because the mortar of band catalyst particles is housed in this reactor, so it is suitable for adopting very active catalyzer very much.
Still it is important that this SBCR reactor is in the very high flexibility that demonstrates aspect operating temperature, product composition, productivity ratio and the operational circumstances.
In the SBCR reactor, gas line speed, catalyst concn and temperature are variable and can bring any big operational issue.Therefore, output and conversion per pass are variable.But in the MTFB reactor, the gas line speed that needs to keep very high is to obtain the favourable interchange of heat between stationary catalyst bed and reactor wall.Therefore, conversion ratio and output can not have any cataclysm.
In the SBCR reactor, can in very wide scope, change product composition (wax/liquor ratio) by changing temperature of reactor.And in the MTFB reactor, just can not do like this, because reaction rate (for given catalyzer) is determined by heat balance.Therefore, mainly be that this MTFB reactor can only be used in the lower temperature range promptly producing the scope of high wax/liquor ratio as 180-220 ℃.In fact, even for the SBCR reactor, the reaction rate that unit effecting reaction body amasss is also definite by heat balance, but in this case, can keep stable heat to generate by changing catalyst concn simultaneously.
Under the situation of unexpected operation as stopping fully under the situation of the synthesis gas device provisioning natural gas of this device, the SBCR reactor can be more durable than MTFB reactor.For the SBCR reactor, this will can not produce big problem, because the liquid phase in the SBCR reactor has very high thermal capacitance, thereby will suppress variations in temperature and other possible operating trouble effectively.But, must damage catalyzer with inert gas purge MTFB reactor in order to avoid owing to temperature is too high.When restarting this device, the catalyzer in the SBCR reactor will suspend when beginning to add synthesis gas simply again, and the MTFB reactor will need more complicated start-up routine, to avoid uncontrollable intensification.
Fig. 2 schematically represents the suitable embodiment of mortar bubble-column reactor 11, and it comprises reactor vessel 12 and fillter section 13.Reactor vessel 12 comprise one usually in a tubular form part 14 and a reverse taper portion 15 above it.Tubular portion 14 constitutes mortar zones 20, admits to contain in this mortar zone 20 and segments in the liquid medium mortar of the catalyzer in the hydrocarbon product for example.This tapering part 15 as an expanding chamber to prevent the foaming of this mortar and overflow and to limit the air chamber 16 above reaction zone.Tapering part 15 can contain other device (not shown) that is useful on destruction or reduces foam formation.
Be provided with an air intake 17 and a gas distributor 18 in the bottom of container 12, this gas can inject the mortar district by this distributor.Be provided with one at the top of container 12 from gas outlet 19 that air chamber 16 comes out.The hot carrier pipe 21 of series connection extends in reactor vessel and between public inlet 22 that is used for heat exchange medium and public outlet 23.Device 11 will wait by many converters, control valve, pump to be controlled, and one of them (pressure or temperature pick up) is for example with 24 expressions.
Fillter section 13 comprises just at 15 times annular outer covers 25 around reactor 12 of tapering part.In shell 25, a part of chamber wall is made by sintering metal and is constituted a filtration members 26 thus.Non-porous 27 of this container stretches into this shell 25 on the top of this shell and bottom.This shell 25 and chamber wall have constituted the air chamber 29 on filtering area 28 and its top effectively.
The outlet of filtering area 28 is as the liquid-level measurement device that is used for filtrate.Pipe 31 extends upward from the outlet 32 near these shell 25 bottoms.Horizontal coupling part 33 has been determined the filtrate plane 34 in filtering area 28 and has been extended downwardly into outlet valve 35.Open valve 35 and emit the liquid form product in lower branch line that accumulates in this pipe.Certainly, can replace downward arm with the jar that holds liquid form product.Liquid form product 33 of opening 32 and horizontal components is housed in outlet 31.
In operation, by gas distributor 18 the gaseous reactant injection is contained the mortar of catalyzer and liquid form product, thereby guarantee that catalyst granules is arranged in suspension.By various sensors for example 24 and heat transfer system 21,22,23 keep the accurate temperature of reaction.Liquid form product is filled in the filtering area 28 by filtration members 26.This can strengthen by the pressure reduction that passes filtration members, and described pressure reduction is to be caused by the hydrostatic head that the difference in level between mortar and the filtrate causes.Keep stable filtrate liquid level 34 according to the upright position of outlet 31 horizontal components 33.
The turbulent motion of mortar helps to prevent to produce filter cake and will avoid filtration members owing to pass the fluctuation or the unstable and situation (wherein valve 39 is opened) that stopped up by catalyst granules of the pressure of filtration members 26.
Remove gaseous products and any unreacted reactant gas by exporting 19.Because tube connector 38 is arranged, thus avoid in air chamber 29 filtrate above accumulate gas.
Can utilize suitable gas such as synthesis gas or suitable liquid such as purified product, or can come cleaning and filtering section 13 by opening valve 37 and shut off valve 35,39.This forces cleaning fluid to return by filtration members 26.
In normal running, the part catalyzer will be removed or by catalyst replaced new or regeneration.For clarity sake, device does not for this purpose illustrate in Fig. 2, but will know that any modular system of used as said purpose can use.
Preferably, around this shell around the part of reactor vessel at least.As shown in Figure 2, this filtration members can be formed by the part wall of this reactor vessel, and this reactor wall is made by filtering material.In another embodiment, this filtration members is discontinuous in reactor outside and this reactor in the filtration members zone.In another case, this filtration members part wall of being arranged in this reactor and this reactor has constituted this shell.Preferably, gas above the mortar phase and the gas above filtrate circulate.
Air chamber above air chamber above the mortar in reaction zone and the filtrate in filtering area is communicated with, and has prevented to produce the pressure reduction that surpasses static pressure thus.This connection can realize by extension usually, and this extension extends between the top of the top of reaction zone and filtering area and these two zones are opened.Preferably, the pipeline that is communicated with this two parts gas will be arranged to such an extent that be convenient to accumulate in the discharge of any gas on the top of filtering area.
Preferably, pass the fluctuation of pressure reduction of filtration members or unsettled scope or size and approximate the average of differential static pressure or more greatly.Preferably, the average pressure reduction that passes filtration members should remain on the quite low numerical value, is generally less than 6 millibars (600Pa).If this average pressure reduction subcritical value (for example 6 person of outstanding talent's crust), this strainer is self cleaning type.
This pressure oscillation value can be the magnitude of this pressure reduction such as the 10-200% of pressure reduction.The actual value of this pressure reduction can be a 1-100 person of outstanding talent crust, is preferably 2-50 person of outstanding talent crust.
Being used for the device of injecting gas reactant or component can comprise any suitable device such as bubble cap column plate, a plurality of nozzle, orifice plate etc., and they preferably are positioned at the bottom of reactor.
As for the more detailed introduction to the SBCR reactor, referring to International Patent Application PCT/NO94/00023, the document is classified list of references as at this.Also with reference to International Patent Application PCT/NO93/00030 and PCT/NO93/00031 and GB-A19317605.
This device is installed on the FPSO device
Method of the present invention is specially adapted to install on the ship of device (FPSO=" floating production, storage and emptying ") of FPSO by name, and this device can be in order to adorn/to be discharged at hydro carbons in the offshore oil and gas producing well, store these hydro carbons and collection, tentatively transforming and refine the hydro carbons that originates from oil well and the floating platform of building and equipping.
In a series of patent and patent application, the applicant has represented and has described the floating platform of the above-mentioned type, is appointed as MST floating platform (MST=" multipurpose oil transportation oil tanker ") herein.Such floating platform is particularly suitable for when the mother ship carrier of the device of implementing the inventive method and can as far as possible neatly and brings into play maximum comprehensive potentiality ground and use such device.
Fig. 3 is a lateral view of schematically representing above-mentioned floating platform.At the front end place of this floating platform, be provided with a unlatching downwards and the cabin of reception under water 40 that receive sub-surface buoy 41, service well 42 is receiving extension between cabin 40 and this floating platform deck 43.Above-mentioned arrangement is so design, promptly can upwards load/unload the sub-surface buoy of hydrocarbon and be fixed in and receive in the cabin (in International Patent Application PCT/NO92/00053, PCT/NO92/00054 and PCT/NO92/00055, more clearly illustrate and described this arrangement) and floating drum can by on draw and fix, described floating drum is suitable for cooperating with the whirligig that is contained in this downhole end, uses (clearer expression and description are arranged) thereby this floating platform is used as the oil recovery floating platform in EP93913638, NO922043 and NO922045.In order to further specify and current related embodiment, at this referring to these publications.
As illustrated, the hand chamber, cabin 44 of this floating platform be arranged on this floating platform fore 45 near.In addition, engine room 46 is placed on below the wheel house with its diesel generation main frame.The service well 42 that extends between floating drum 41 and this floating platform deck 43 is just in the back of wheel house, thereby the crewman that will go into the well will be positioned at the leeward side behind the wheel house.
At this charge of oil multichannel pipe/swivel joint 47 that is connected with floating drum 41 has been installed above the floating drum, has also been installed one thereon and had tubing valve 48 tube connectors.The checkout gear 49 that also drawn is used at switch 50 and a guiding device 51 that is used for drawing this floating drum of receiving closed-in well 42 above the cabin as TV video camera, one.On this deck, also installed one and lifted winch 52, a storage device 53 and an especially relevant maintenance crane 54 with maintenance.A pair of bow thruster 45 has been installed in the fore of this floating platform.
The treating apparatus that is used for processing oil is installed in the balladeur train on the deck between the front and rear of this floating platform.Originate from the oil field and deliver to from oil field and sub-surface buoy 41 by standpipe that logistics is separated into the water, oil, gas body at this in the well of this floating platform.Represent this device with the form of many portable cabins 56.Heap has many loadings cabin or jar 58 between the front and rear of this floating platform.In this Background Region, also be provided with a torch burning arm 57.
Fig. 4 is that to be equipped with the association conversion of natural gas be the phantom drawing of oil recovery floating platform of apparatus of the present invention of synthetic crude and/or wax.This device is installed in wheel house back in the fore portion of this floating platform and all are used for receiving the back of the reception cabin (not shown) of loading buoy under water.
An importance of the preferred embodiment of apparatus of the present invention is that this device is applicable to the technology that constitutes MST floating platform basis fully and is combined into an integral body with such technology.In a preferred embodiment, this floating platform has this device.This especially means: this Design of device and structure and the size that is used for the oil recovery floating platform skeleton of cabin formula structure adapt; Adjust the structure of described device according to the substructure of oil recovery floating platform, described substructure comprises for example center pipe support; Described Design of device is in structure and provide the various accessory systems of cooling water, water vapour, oxygen etc. to adapt.In addition, in principle, this device should all be applicable to best under any supposition situation and oil recovery particularly adapt with association amount of natural gas of being produced and natural gas injection rate.Because of this device and accessory system are self-contained within the advantage that obtains on the oil recovery floating platform ship especially the unconverted gas of this device can be used for the power plant generating or desalinization is handled.Also advantageously, from the product of FT reactor isolated and contain acid (for example acetate) and alcohol (for example methyl alcohol) big water gaging can be used for oil-field flooding.Also having an advantage is the seawater that is easy to obtain cooling off usefulness.
Device of the present invention suitably has 420-21000 bucket C
5+/ day (53.5-2675 ton C
5+/ sky) productivity, this is equivalent to 0.1-5.0 1,000,000 Sm
3The gas material in/sky.Preferred productivity is 2100-8400 bucket C
5+/ day (267.5-1070 ton C
5+/ day), it is equivalent to 0.5-2.0 1,000,000 Sm
3The gas material in/sky.Significant especially device size is and is about 4200 barrels of C
5+/ day (about 535 tons of C
5+/ sky) productivity correspondence, above-mentioned productivity is equivalent to 100 ten thousand Sm
3The natural gas in/sky.
Can and therefore load onto ship with the crude oil mixing of originating from oil well by synthetic crude and/or wax product that this device makes with crude oil.In addition, the product of this device can be transferred in each product storage tank so that respectively from unloading of oil recovery floating platform and sale/refining respectively.Under many circumstances, this may be favourable, and this is because the product that obtains from the synthesis gas of producing this device is better than common crude oil in quality and properties usually, especially because of its sulfur-bearing not in fact.Therefore, for example this crude oil is suitable as the diesel oil of production high cetane number and the raw material of various high-quality lubricating oil components.
Another advantage of described skid-mounted unit is: when not using it on oil recovery floating platform ship, it can be installed on the suitable synthetic crude continental rise process units.
It is significant place as factory's raw material that the similar device that is not suitable for the MST floating platform can be used for special-purpose floating platform, permanent offshore installation or the place of pulling in to shore such as long-range natural gas.
Below, as a simulation embodiment who has described the Fischer-Tropsch composite part of the inventive method of in shown in Figure 2 and device as above brief introduction, implementing with working embodiment.
Work embodiment
Adopt that the applicant developed be used for mortar bubble-column reactor (SBCR reactor) and based on the reaction dynamics data of following catalyzer with in the quality transmission of mortar bubble column and the Mathematical Modeling of fluid dynamic generally acknowledged relation, for the work of the Fischer-Tropsch composite part of as shown in Figure 2 apparatus of the present invention provides data, it comprises the SBCR reactor of two series connection and remove the water and the C of condensation in reactor
5+So that from synthesis gas, produce liquid hydrocarbon (C
5+).
In reactor, used the Co that contains 20% (percentage by weight) and 1% Re's and with γ-Al
2O
3Cobalt-rhenium catalyst for carrier.The catalyzer of introducing in US4801573 is with Co (NO according to the incipient wetness method
3)
26H
2O and HReO
4Aqueous solution dipping γ-Al
2O
3Preparing carriers.
Synthesis gas with composition that following table 1 provides with 153,000Sm
3The supply of/h is injected first reactor (reactor 1) of two tandem reactors.Described synthesis gas supply is equivalent to supply with about 100 ten thousand Sm of this device reformation tower section
3The natural gas in/sky and the recovery synthesis gas sum of exporting by SBCR reactor 2.The composition of synthesis gas is typically by the composition of the synthesis gas that makes in the long-range natural gas.
The condition of work and the key data of two reactors 1,2 have been provided in the table 2 below.
Table 3 has provided the various logistics capacities of input and output reactor 1,2.
CO conversion per pass total amount in two reactors is 89%.
The composition composition mole % of the synthesis gas of table 1 input reactor 1
H
2 58．3
H
2O 0．3
CO 29．0
CO
2 11．6
N
2 0．5
CH
4 0．3
The data of table 2 mortar reactor
1) height 2 of expansion mortar) in the entrance 3) average 4) be converted into C
5+The total mole number of CO of CO molal quantity/conversion
| Reactor |
| 1 | Reactor 2 | |
| (m) 1 highly) | 10 | 10 |
| Diameter (m) | 5．8 | 3．9 |
| Gas line speed (m/s) 2) | 0．1 | 0．1 |
| Temperature of reactor (℃) 3) | 230 | 230 |
| Gross pressure (crust) | 30 | 28 |
| Catalyst concn (percentage by weight) | 20 | 20 |
| Conversion ratio (CO) (%) | 66．5 | 67．0 |
| Reactor productivity ratio (kgHC/m 3h) | 70 | 50 |
| Catalyst productivity (kgHC/kg cat.h) | 0．50 | 0．37 |
| To C 5+Selectivity (%) 4) | 88 | 87 |
Table 3 logistics capacity (ton/hour)
| | Reactor | 1 | | |||
| Input | Output | Input | Output | |||
| H 2 | 8.0 | 2.6 | 2.6 | 0.8 | ||
| H 2O | 0.3 | 23.5 | - | 7.7 | ||
| C0 | 55.4 | 18.5 | 18.5 | 6.1 | ||
| CO 2 | 35.0 | 35.6 | 35.6 | 36.0 | ||
| N 2 | 0.9 | 0.9 | 0.9 | 0.9 | ||
| CH 4 | 0.3 | 1.3 | 1.3 | 1.7 | ||
| C 2-C 4 | - | 1.2 | 1.2 | 1.6 | ||
| C 5+ | - | 16.3 | - | 5.3 | ||
Claims (7)
1. one kind is suitable at sea and at floating platform, carry out on platform or other device, with natural gas, particularly two steps of association natural gas are converted into the method for synthetic crude and/or wax, wherein (1) is described conversion of natural gas by carbon monoxide in the synthesis gas device, the synthesis gas that the mixture of hydrogen and carbon dioxide is formed, (2) in the Fischer-Tropsch synthesizer, this synthesis gas is converted into synthetic crude and/or wax, it is characterized in that, for carry out the synthetic synthesis gas that obtains by step (1) of Fischer-Tropsch with a kind of by liquid form product, the form of the mortar that segmentation catalyst granules and synthesis gas are formed is injected the reaction zone of mortar bubble-column reactor (SBCR reactor), in this reactor liquid form product is separated inside from the remainder of mortar.
2. according to the method for claim 1, it is characterized in that: synthesis gas that cooling is obtained by step (1) and the reaction zone that after dehydration, is injected into mortar bubble-column reactor bottom, said reaction zone be arranged to be suitable for holding the mortar formed by liquid form product, segmentation catalyst granules and the synthesis gas of being supplied with at the gas of this mortar above mutually; With the fillter section that comprises shell and filtration members liquid form product is separated from the remainder of mortar, described shell and filtration members have constituted a filtering area with filtrate product outlet, and said filtration members is contacted with mortar in the reaction zone; At filtering area be included in this mortar gas above mutually and between interior reaction zone part, set up the fluid flow relation; The even pressure reduction of this filtration members is passed in formation.
3. according to the method for claim 1 or 2, it is characterized in that: in step (1), realize by partial oxidation by the conversion of natural gas to synthesis gas.
4. one kind with natural gas, particularly two steps of association natural gas are converted into the device of synthetic crude and/or wax, wherein (1) is this conversion of natural gas by carbon monoxide in the synthesis gas device, the synthesis gas that the mixture of hydrogen and carbon dioxide is formed, (2) in the Fischer-Tropsch synthesizer, the synthesis gas that is obtained by described device is converted into synthetic crude and/or wax, it is characterized in that: this Fischer-Tropsch synthesizer comprises one or more mortar bubble-column reactors (SBCR reactor), each reactor comprises a reaction zone, and this reaction zone is arranged to be suitable for holding by liquid form product, the mortar that segmentation catalyst granules and synthesis gas are formed and this reactor are arranged to be suitable for from the remainder of mortar inside and isolate liquid form product.
5. according to the device of claim 4, it is characterized in that: each mortar bubble-column reactor comprises: one constitute one arrange be suitable for holding mortar mutually with container at the reaction zone of the gas of mortar above mutually; Inject the device of synthesis gas in mutually at the mortar of this container bottom; Layout is used for isolating mutually from mortar the fillter section of liquid form product, this fillter section comprises a shell and the filtration members to small part around this container, this filtration members constitutes a filtering area that has the filtrate product outlet with said shell, and described filtration members is arranged to contact with mortar in the mortar district; Form the device that circulates between the reaction zone part that when filtering area and use, is occupied at the gas above the mortar phase; The device of the even pressure reduction of this filtration members is passed in formation.
6. according to the device of claim 5, it is characterized in that: this device is fixed on the balladeur train of floating platform, offshore platform or other offshore installation with being positioned at easy replacing.
7. according to the device of claim 6, it is characterized in that: this device is suitable for being installed on the FPSO floating platform (FPSO=" floating production, storage and emptying ").
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NO953797A NO953797L (en) | 1995-09-25 | 1995-09-25 | Process and plant for treating a brönnström produced from an offshore oil field |
| NO953797 | 1995-09-25 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1200786A CN1200786A (en) | 1998-12-02 |
| CN1060839C true CN1060839C (en) | 2001-01-17 |
Family
ID=19898597
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96197901A Expired - Fee Related CN1060839C (en) | 1995-09-25 | 1996-09-25 | Method and equipment for treating well stream from offshore oil field |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP0852656A1 (en) |
| CN (1) | CN1060839C (en) |
| AU (1) | AU696493B2 (en) |
| BR (1) | BR9610694A (en) |
| CA (1) | CA2232867A1 (en) |
| EA (1) | EA000650B1 (en) |
| NO (2) | NO953797L (en) |
| WO (1) | WO1997012118A1 (en) |
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- 1996-09-25 AU AU71001/96A patent/AU696493B2/en not_active Ceased
- 1996-09-25 WO PCT/NO1996/000227 patent/WO1997012118A1/en not_active Application Discontinuation
- 1996-09-25 EA EA199800339A patent/EA000650B1/en not_active IP Right Cessation
- 1996-09-25 CA CA002232867A patent/CA2232867A1/en not_active Abandoned
- 1996-09-25 BR BR9610694A patent/BR9610694A/en unknown
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-
1998
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| WO1994000333A1 (en) * | 1992-06-29 | 1994-01-06 | Kvaerner A.S | A device for the production of oil/petroleum products at sea |
Also Published As
| Publication number | Publication date |
|---|---|
| NO981271D0 (en) | 1998-03-20 |
| MX9802328A (en) | 1998-08-30 |
| WO1997012118A1 (en) | 1997-04-03 |
| NO981271L (en) | 1998-03-20 |
| AU696493B2 (en) | 1998-09-10 |
| EP0852656A1 (en) | 1998-07-15 |
| BR9610694A (en) | 1999-07-06 |
| EA199800339A1 (en) | 1998-12-24 |
| NO953797L (en) | 1997-03-26 |
| AU7100196A (en) | 1997-04-17 |
| EA000650B1 (en) | 1999-12-29 |
| CA2232867A1 (en) | 1997-04-03 |
| CN1200786A (en) | 1998-12-02 |
| NO953797D0 (en) | 1995-09-25 |
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