EA000650B1 - Method and system for the treatment of a well stream from an offshore oil field - Google Patents

Abstract

1. A process - for being carried out offshore on a vessel, a platform or other installation - for conversion of a natural gas, especially an associated natural gas, to a synthetic crude oil and/or wax in two stages, wherein (1) the natural gas is converted to a synthesis gas consisting of a mixture of carbon monoxide, hydrogen and carbon dioxide in a synthesis gas unit, and (2) the synthesis gas is converted to a synthetic crude oil and/or wax in a Fischer-Tropsch synthesis, characterized in that the synthesis gas from stage (1) for the carrying out of a Fischer-Tropsch synthesis is introduced, in a slurry consisting of liquid products, finely divided catalyst particles and synthesis gas, into a reaction zone in a slurry bubble column reactor (SBCR reactor) wherein an internal separation of the liquid products from the remaining part of the slurry is effected. 2. A process according to Claim 1, characterized in that the synthesis gas from stage (1), after cooling and separation of water, is introduced into the bottom of the reaction zone in the slurry bubble column reactor, said reaction zone being arranged to accommodate for the slurry consisting of liquid products, finely divided catalyst particles and supplied synthesis gas, and to accomodate for a volume of gas above the slurry phase; that liquid product is separated from the remaining part of the slurry by means of a filtration section including a housing and a filter element which together define a filtrate zone having an outlet for the product filtrate, said filter element being arranged to be in contact with the slurry in the reaction zone; that fluid communication is established between the filtrate zone and the portion of the reaction zone containing the gas volume above the slurry phase; and that a mean pressure differential is established across the filter element. 3. A process according to Claim 1 or 2, characterized in that the conversion of natural gas to a synthesis gas in stage (1) is effected by partial oxidation. 4. A plant for conversion of a natural gas, especially an associated natural gas, to a synthetic crude oil and/or wax in two stages, wherein (1) the natural gas is converted to a synthesis gas consisting of a mixture of carbon monoxide, hydrogen and carbon dioxide in a synthesis gas unit, and (2) the synthesis gas from said unit is converted to a synthetic crude oil and/or wax in a Fischer-Tropsch unit, characterized in that the Fischer-Tropsch unit comprises one or more slurry bubble column reactors (SBCR reactors) each comprising a reactor zone arranged to contain a slurry consisting of liquid products, finely divided catalyst particles and synthesis gas, and in that the reactor(s) is/are arranged for internal separation of liquid products from the remaining part of the slurry. 5. A plant according to Claim 4, characterized in that each slurry bubble column reactor comprises: a vessel defining a reaction zone arranged to accommodate both the slurry phase and a volume of gas above the slurry phase; means for introducing the synthesis gas in the slurry phase in the lower region of the vessel; a filtration section arranged to separate liquid products from the slurry phase, including a housing which at least partially surrounds the vessel, and a filter element which together with said housing defines a filtrate zone having an outlet for the product filtrate, said filter element being arranged to be in contact with the slurry in the slurry zone; means establishing fluid communication between the filtrate zone and that part of the reaction zone which in use is to be occupied by the volume of gas above the slurry phase; and means for establishing a mean pressure differential across the filter element. 6. A plant according to Claim 5, characterized in that it is located on skids which can be secured easily exchangeably to a vessel, an offshore platform or other offshore installation. 7. A plant according to Claim 6, characterized in that it is adapted for installation on a FPSO vessel (FPSO = "Floating Production, Storage and Offloading").

Description

Technical field

The present invention relates to a method and system for processing a stream from a well produced from an oil field on the high seas. The present invention also relates to a method for converting natural gas, in particular bound natural gas, into synthetic crude oil by Fischer-Tropsch synthesis, which is to be carried out in the open sea on a ship, platform or other installation. The present invention also relates to a system for implementing such a method located on easily replaceable runners, especially for installation on an FPSO vessel (FPSO - Production, storage and unloading in a floating state).

State of the art

Extraction of crude oil from the offshore oil field requires separation of the flow from the oil well into water, oil and gas. Natural gas, which accompanies the produced crude oil in a stream from an oil well and which is often referred to as bound gas, must be treated in one way or another after its separation. Such treatment often involves burning gas or re-injecting gas into an oil field, but it can also be transported ashore for further processing. Gas burning is an unacceptable way to remove gas, since such burning represents losses of gradually decreasing hydrocarbon reserves and is also a source of air pollution. Re-injection, which increases the cost of producing crude oil, is in most cases unacceptable because of the costs and possible undesirable effects on the production of oil from an oil field. A third solution to the problem, that is, transporting gas from an oil field, for example through a pipeline, for processing in a surface installation, is an expensive and impractical solution, at least from remote oil fields.

A well-known method in essence is the conversion of natural gas to synthesis gas (CO + H ₂ ) and the conversion of the latter into synthetic crude oil by Fischer Tropsch synthesis, which is described in the exhaustive literature, see, for example, G.A. Mills, Status and Future Opportunities for Transforming Synthesis Gas into Liquid Fuel, Volume 73 (8), pp. 1243-79 (1994), Journal of Fuel. In the last 80s, interest again appeared in this method for treating gas transported ashore from oil fields on the high seas, that is, in South Africa and Malaysia. However, as the present applicants are well aware, any installation based on Fischer Tropsch technology has not yet been installed in the open sea, for example, on platforms, jacks, floating vessels for oil production, storage and unloading, including, for example, production vessels and shuttle tankers ; FSU installations (FSU - installation for storage in a floating state), for example, semi-submersible platforms, etc.

Recently, shuttle tankers have become known that are designed so that they themselves can be connected to submarines that simultaneously hold the ship anchored. Such submarine cargo buoys form a collection point for one or more vertical pipes and umbilical cords, for example, from a mining system at the bottom of the sea. Buoys are adapted for lifting and securing on a ship of local importance to establish a system for transporting oil products from the system at the bottom of the sea, for example, to cargo tanks on a ship.

With this technology, as a starting point, recently built ships that can be changed with simple means to work as:

a) a shuttle tanker which itself is connected to an underwater cargo buoy,

(b) a storage vessel permanently connected to an underwater cargo buoy that has simultaneously unloading equipment at the stern of the vessel for unloading oil; and

c) a production vessel that is connected to an underwater cargo buoy containing a swivel.

A vessel of this type, based on interaction with an immersed cargo buoy fixed on the bottom of the sea, which may contain a swivel mechanism having several rows of pipes, is described in Norwegian patent No. 940352. Near its front end, the vessel has an immersed receiving space for receiving an immersed buoy and a shaft for service, passing between the receiving space and the deck of the vessel. The buoy has an external floating element, which is adapted for insertion and removable fastening in the submerged receiving space, open downward in the vessel, and a central element mounted for rotation on the external element and fixed on the bottom of the sea and connected to at least one transmitting a line from the corresponding production well up to the buoy.

When a buoy of this type is fixed in the receiving space on the vessel, the vessel is rigidly connected to the external floating element of the buoy and rotationally around the central element of the buoy, which is fixed to the bottom of the sea with an appropriate anchoring system. Thus, the buoy itself forms a rotating body or tower around which the ship can rotate under the influence of wind, waves and water currents.

This buoy design has several significant advantages. The central element of the buoy has a small diameter and a small mass, thus achieving a correspondingly small diameter of the rotating body, i.e. an external buoyant buoy element and therefore a small rotating mass and rotation resistance. The operations of connecting and disconnecting between the vessel and the buoy can be carried out in a simple and quick way, even in bad weather with relatively high waves. The buoy can also remain connected to the ship under almost all weather conditions, and if weather limits are exceeded, the ship can be quickly disconnected.

In a vessel that is intended to be used with the aforementioned buoy structure, the receiving space and the shaft located above it are located respectively in the bow of the vessel. This makes it relatively easy to convert existing vessels to fit them into such a buoy loading system for use, for example, as shuttle tankers. The combination of the immersed receiving space and the shaft, which is located between the receiving space and the deck of the vessel, can also ensure high reliability of the system in operation and reduce the risk of polluting leaks.

For a more complete description of the aforementioned construction of a buoy and a vessel of the aforementioned type, reference may be made to International Patent Applications No. PCT / NО 92/00054, PCT / NО 92/00055 and PCT / NО 92/00056.

The preferred use of such a buoy loading system for offshore oil production and gas production on a production vessel is described in Norwegian Patent No. 922043. In the design described in this patent, the system comprises a swivel mechanism that is designed to lower or raise it from its working position at the lower end of the shaft and for connection in the working position with the piping system on the ship. The swivel mechanism comprises inner and outer mutually rotating swivel elements. At the upper end of the buoy is a connecting device or connector in which the current number of transmission lines ends, and this connecting device is adapted to connect and accordingly disconnect the corresponding connecting means on the underside of the swivel mechanism.

In a preferred embodiment of the present system, the swivel mechanism is located on a raising and lowering tool, which is slidably mounted on a guide rail extending between the upper and lower ends of the shaft. Thus, the swivel mechanism with its connector or connecting device can be placed in a simple way in the correct position in the connecting cavity or space at the lower end of the shaft. Since they are the most critical elements, the swivel mechanism and the connecting device will be easily accessible for maintenance or replacement. The connection and disconnection from the buoy transmission lines can be carried out as a one-step operation with automatic closing dampers on both sides of the connecting devices. The vertical movement of the swivel mechanism during connection and disconnection can be absorbed by typically flexible pipes that are positioned at right angles to the axis of the swivel mechanism.

A significant advantage of this system is that it is small due to the use of a special buoy, which itself forms a rotating body. The result is weight savings and reduced equipment volume, which significantly reduces costs.

Such a system requires minimal rebuilding of shuttle tankers that are adapted for the aforementioned loading of the buoy for transportation to production vessels. With such a production vessel, seasonal operations can also be carried out in addition to continuous production in oil fields on the high seas and also trial production. The vessel can be used, for example, for trial production during the summer months, during a period having a possible surplus of shuttle tankers.

As a result of the fact that the wheelhouse of the vessel and its engine room are located in the bow of the vessel, and the shaft for service from the receiving space of the vessel is located immediately behind the wheelhouse, the shaft for maintenance will be located on the leeward side of the wheelhouse. In addition to ensuring reliability, it also provides a large deck area from the rear of the wheelhouse and back to the rear of the deck for the team to perform tasks in the mine. When a vessel is to be used as a production vessel, this area can be used to accommodate the necessary technological equipment and equipment for monitoring the well.

Since this vessel can be changed between different areas of activity, it is preferable to divide all technological equipment into small portable modules.

As described above, such a vessel is very suitable for transporting a plant for converting bound natural gas, for example, into synthetic crude oil and / or paraffin. In addition, such a device provides advantages resulting from the presence of a system with a swivel mechanism, also suitable for use in conjunction with installations for water injection, water treatment, well stimulation, etc., which allows the use of a vessel with a high degree of flexibility. This system is also suitable for use in waters contaminated by drifting ice and icebergs, as it can be quickly disconnected when necessary without risk of damage to the submerged buoy.

As mentioned in the introduction, the present inventors are not aware of the existence of any installation located on the high seas, which is based on Fischer-Tropsch technology. However, modular plants for converting gas, or systems for converting bound natural gas or removing gas to be converted into synthetic crude oil, which are placed on ships, platforms or other offshore installations are described by Dr. David D. J. Antia and Dr. Duncan Seddon in their work Using new opportunities to reduce costs and increase profits by converting offshore gas into crude oil presented at the conference (Strategy and Economics in the North Sea), London, 2 November 8-29, 1994

This publication describes modular plants or systems for converting gas that can be connected to new and existing offshore oil production systems. Modular plants are suitable for converting natural gas into synthetic crude oil, paraffin or methanol. This publication is directed, in particular, to the description of installations intended for use in oil fields producing from 5 to 50 million cubic feet / day (0.14 - 1.42 million m ³ / day) of bound gas. This article defines two types of installations:

(a) plants designed to profit from gas before it is re-injected into the field; and (b) plants designed to fully process gas by turning it into more easily manageable and valuable products to prevent gas burning, re-injection or removal.

In plants of these two types, the method consists of two main steps: (1) natural gas is converted into synthesis gas, consisting of a mixture of carbon monoxide, hydrogen and carbon dioxide in a partial oxidation plant, and (2) the synthesis gas is converted into synthetic crude oil in the Fischer-Tropsch reactor. It should be noted that the present method is a flexible method that allows you to switch during operation to other end products, from light condensate to microcrystalline paraffin.

Equipment for the implementation of the two-stage method can be placed in separate modules or in groups of modules mounted on runners. It should be noted that the installation of the installation on a modular basis provides flexibility, reflected, for example, by the productivity of the installation, which should increase or decrease when required, or by the productivity of the installation, working with parallel flows producing various products, for example, synthetic crude oil, paraffin and methanol.

To obtain synthesis gas from natural gas in the first stage of the process, several methods are used from the publication of Antia et al. The most important of them are partial oxidation, vapor phase reforming, autothermal reforming in the presence of a catalyst, and combined reforming. Partial oxidation is preferable based on the efficiency of the method, cost, flexibility in the composition of the product, installation size, product yield, organization (logistical support) and economics.

To produce synthetic crude oil and / or paraffin in the second stage of the process, i.e. Fischer-Tropsch synthesis, a number of different types of reactors can be used, for example, reactors that are multi-tube fixed-bed reactors (MTFB = multi-tube fixed-bed reactor) reactors with a bed of fluidized material, reactors with an annular layer, reactors with a suspended catalyst and an isothermal reactor Linde. Among these reactors, Antia et al., A fixed-bed multi-tube reactor is preferred because it is tested, cheap and flexible, and can operate over a wide temperature range. In the mentioned publication it is indicated that a reactor with a suspended catalyst was thoroughly investigated, but it did not justify itself from a technical point of view.

The Fischer-Tropsch synthesis reactor uses an iron, cobalt or ruthenium catalyst. It can be said that all of these types of catalysts can form products having a composition ranging from light condensates to heavy paraffin oils or microcrystalline or paraffin wax.

Thus, even if the majority of the foundations are based on economically viable processing of bound natural gas without harming the environment by turning it into valuable and more easily manageable products, however, there is still a need for improved solutions to achieve safer and more profitable operations.

The use of the aforementioned fixed-bed multitube reactor, which is considered by Antia et al. To be the preferred reactor for use in the Fischer-Tropsch synthesis, is hindered to a large extent by its disadvantages, such as its large weight, expensive and complex construction, and narrow range of working temperatures. To maintain the pressure drop across the catalyst bed to an acceptable level in a fixed-bed multitube reactor, large catalyst particles must be used, which entails limitations in diffusion. For this reason, and because of the difficulty in controlling the temperature in the reactor, the conversion of synthesis gas in one pass becomes lower than required. In addition, the replacement of the catalyst in a reactor of this type is complicated, and the reactor is not suitable for highly active catalysts.

Objectives of the present invention

In view of the prior art, it is an object of the present invention to provide a method and system for processing on board a stream of oil produced from a well in an offshore oil field using the vessel in conjunction with an underwater buoy to which the vessel and vertical pipes from the oil field are attached.

Further, the aim of the present invention is to develop a method for converting natural gas, in particular natural bound gas, into synthetic crude oil and / or paraffin suitable for its implementation in places with limited space, for example, on a vessel, platform or other installation located in an open sea.

Further, the aim of the present invention is to provide a simple, compact and reliable installation for converting natural gas into synthetic crude oil and / or paraffin. More specifically, it is an object of the present invention to provide such a plant for converting bound natural gas, which is mounted on skids and which can be easily fixed on a ship with the possibility of replacing it, on an offshore platform or other installation located in the open sea, in particular on a floating a vessel intended for oil production, storage and unloading.

A further object of the present invention is to provide a plant of the type mentioned, which can be easily reconstructed to produce products having different specifications, and which can also be easily redone in relation to its productivity.

SUMMARY OF THE INVENTION

According to a first aspect of the present invention, there is provided a method for processing onboard a stream of a well produced from an offshore oil field using a vessel interacting with an underwater buoy to which the vessel and vertical pipes extending from the oil field are attached, with a swivel located above the buoy mechanism on the ship. The present method is characterized in that it includes the stages of directing the flow from an oil well to a processing unit located on easily replaceable runners attached to the deck of the vessel on either side of the tubular stand located longitudinally in the center on the vessel, separating water, oil and gas from one another from a friend in a processing unit, storing separated stabilized oil in at least several reservoirs for storing oil on board the vessel and directing the separated gas to the installation for converting gas into synthetics eskuyu crude oil and / or paraffin, which is then stored in storage tanks in the vessel, the synthetic crude oil may be mixed with stabilized oil.

According to another aspect of the present invention, there is provided an apparatus for processing a stream from an oil well extracted from an offshore oil field, which is installed on board a vessel and comprises processing equipment in which water, oil and gas are separated from each other. The present installation is characterized in that it also contains equipment for converting the separated gas to synthetic crude oil and / or paraffin, said gas converting equipment comprising at least one gas synthesis device and a Fischer-Tropsch device, and the entire installation ( technological equipment and equipment for transformation) is located on runners that can be easily attached with the possibility of their replacement to the deck of the vessel.

According to yet another aspect of the present invention, there is provided a method, in particular for implementation on a ship, platform or other installation located on the high seas, for converting natural gas, in particular bound natural gas into synthetic crude oil and / or paraffin in two stages in which (1) natural gas is converted into synthesis gas, consisting of a mixture of carbon monoxide, hydrogen and carbon dioxide, in a device for the formation of synthesis gas and (2) synthesis gas is converted into synthetic crude oil and / or paraffin Fischer-Tropsch synthesis. The present method is characterized in that the synthesis gas from stage (1) for the synthesis according to the Fischer-Tropsch method is introduced into a suspension consisting of liquid products, finely divided catalyst particles and synthesis gas into the reaction zone of the reactor with a distillation (cap) column with catalyst mixture (KCRK reactor), in which the internal separation of liquid products from the rest of the suspension.

In a preferred embodiment of this method, the synthesis gas from step (1) is introduced after cooling and separating water into the lower part of the reaction zone of a distillation column reactor with a catalyst mixture, said reaction zone being arranged to receive a suspension consisting of finely divided liquid products particles of the catalyst and the supplied synthesis gas, and the volume of gas above the suspension phase, the liquid product is separated from the rest of the suspension by means of a filter section including a housing and a filter element nt, which together form a filtrate zone having an outlet for product filtrate, the filter element being positioned to be in contact with the suspension in the reaction zone, a fluid communication is established between the filtrate zone and the part of the reaction zone containing the gas volume above the suspension phase , and an average pressure drop is created through the filter element.

According to another aspect of the present invention, there is provided an apparatus for converting natural gas, in particular bound natural gas, into synthetic crude oil and / or paraffin in two stages, in which (1) natural gas is converted to synthesis gas consisting of a mixture of carbon monoxide , hydrogen and carbon dioxide, in syngas equipment, and (2) the synthesis gas from this equipment is converted to synthetic crude oil and / or paraffin in a Fischer-Tropsch plant. This installation is characterized in that the Fischer-Tropsch installation contains one or more reactors with a distillation column with a catalyst mixture (KCRK reactors), each of which contains a reaction zone designed to contain a suspension consisting of liquid products, finely divided particles of the catalyst and synthesis gas and the reactor (s) are installed for the internal separation of liquid products from the rest of the suspension.

The installation in its preferred embodiment is characterized in that each reactor with a distillation column with a catalyst mixture contains a vessel forming a reaction zone designed to contain the suspension phase and the gas volume above the suspension phase, means for introducing synthesis gas in the suspension phase in the lower region of the vessel, a filtering section for separating liquid products from the suspension phase and comprising a housing that surrounds at least partially the vessel, and a filter element, which together with the said body catfish forms a filtrate zone having an outlet for product filtrate, and the filter element is located so as to be in contact with the suspension in the suspension zone, means for establishing fluid communication between the filtrate zone and that part of the reaction zone that should be occupied by volume during use gas over the suspension phase, and a means of establishing an average pressure drop through the filter element.

In preferred embodiments, the installation is located on runners that can be easily fixed and can be replaced on a ship, offshore platform or other installation located on the high seas, in particular, on a floating vessel designed for the extraction, storage and unloading of oil.

Brief Description of the Drawings

FIG. 1 is a simplified flow diagram for an embodiment of a method according to the present invention.

FIG. 2 is a schematic cross-sectional view of a distillation column reactor with a catalyst mixture for use in a Fischer-Tropsch synthesis plant in the method of the present invention.

FIG. 3 is a perspective view, partially in section, of a cargo and production vessel having a loading system using a hydrocarbon loading buoy and a space for installing a system for implementing the method of the present invention.

FIG. 4 is a perspective view of a production vessel having a modular system according to the present invention for installation on board a vessel.

Detailed description of the present invention

Next will be described with reference to the attached FIG. 1, the main features of a preferred embodiment of a two-stage method and system according to the present invention for converting natural gas, in particular bound natural gas, into synthetic crude oil and / or paraffin. Bound gas under a pressure of about 40 bar is heated to a temperature of about 400 ° C and introduced into the absorption column 1, in which sulfur, present only in the form of H ₂ S, is absorbed in the layer of ZnO particles. The desulfurized gas from the absorption column is mixed with steam and the mixture is heated to a temperature of about 500 ° C and introduced into the autothermal reforming unit 2. The oxygen extracted from the air is mixed with steam and introduced at a temperature of about 300 ° C into the autothermal reforming unit. Recycling gas from synthesis according to the Fischer-Tropsch method, heated to a temperature of about 300 ° C, is also introduced into the reforming unit. Autothermal reformingustanovka comprises a burner in which the mixed reagents combustion zone in which combusted hydrocarbons with oxygen to produce CO and H ₂ O, heat zone and a subsequent zone packed with the catalyst, in which is converted to CO and H2 remaining hydrocarbons and water, and where an equilibrium is established between CO and H ₂ O, on the one hand, and an equilibrium between CO ₂ and H ₂ , on the other hand (the reaction of a change in the ratio of carbon monoxide and hydrogen in water gas). To achieve a molar ratio of H ₂ : CO in the range from 1.6: 1 to 2.0: 1 at the exit from the autothermal reforming unit 2, the relations between the reactants and other reaction conditions are regulated.

The synthesis gas removed from the autothermal reforming unit is rapidly cooled to a temperature of about 300 ° C. by direct injection of water into the gas. The synthesis gas is also cooled in a heat exchanger, and water is separated from it (not shown). The synthesis gas is then introduced at a temperature of about 200 ° C. into the Fischer-Tropsch synthesis plant, which consists of two reactors 3, as shown in this drawing. The components of the synthesis gas react with each other in an exothermic process, forming hydrocarbons and water. Fischer-Tropsch synthesis reactors are distillation column reactors with a catalyst slurry. The term suspension, as used here, means a three-phase mixture of solid catalyst particles, liquid hydrocarbons consisting of products from the Fischer-Tropsch synthesis step, and a gas consisting of unreacted reactants and gaseous hydrocarbons formed during the Fischer-Tropsch synthesis. Excess heat is removed by heat exchange with water circulating through heat exchanger tubes located inside the reactors with a distillation column with a catalyst suspension 3. Under reaction conditions that include a temperature of about 230 ° C, hydrocarbons will be present both in the gaseous phase and in the liquid phase. The unreacted synthesis gas and gaseous hydrocarbon product are removed from the upper part of the reactors 3. A filtration system located in the upper part of the reactor separates the catalyst from the liquid products.

Gaseous products from reactors 3 are cooled (not shown in the drawing) and introduced into a separator 4 to separate water and a liquid stream consisting of synthetic crude oil, which is the desired product. Part of the separated water is recycled to the inlet of the reforming unit 2. Part of the non-condensed gas removed from the separator 4 is recycled to the inlet of the reforming unit 2, while the rest of this gas can be used as combustible gas to heat the feed to the autothermal reforming -installation and / or use it to generate energy in electric generators or to produce fresh water from sea water. Part of this condensed gas can also be used for injection purposes.

The two reactors 3 with a distillation column with a catalyst slurry and feed shown in this drawing are connected in series, but they can also be connected in parallel, as indicated by dashed lines in the drawing. When reactors are connected in series, reaction water and liquid hydrocarbons (C ₅ +) can be removed respectively from the product stream downstream of the first reactor to increase the efficiency of the second reactor. If necessary, then each reactor 3 can operate separately.

In catalyst distillation column reactors in the system of the present invention, any catalyst suitable for use in Fischer-Tropsch synthesis for the production of synthetic crude oil and / or paraffin, for example, a catalyst from iron, cobalt, nickel or ruthenium, can be used. previously known for such an application. A preferred catalyst is a cobalt-rhenium supported alumina catalyst. The metal from the group of rare-earth metals can enhance the action of the catalyst. For example, a cobalt-rhenium catalyst containing 20% by mass of Co and 1% by mass of Re per γ-Α _{1 2} Ο _{3 can be used} . Such a catalyst is described in US Pat. No. 4,801,573, and can be prepared by impregnating γ-Ο12Ο3 with an aqueous solution of SODOD · 6H ₂ O and HReO ₄ according to the method of rudimentary moisture.

When using the preferred catalysts for synthesis according to the Fischer-Tropsch method, more than 85% CO conversion in one pass is achieved (up to 98% can be achieved), more than 88% C5 selectivity and α polymerization probability, according to Anderson-Schultz-Flory distribution, 0.9-0, 95.

The combination of the preferred catalysts and the described reactors with a distillation column with a catalyst suspension and feedstock provides high C5 selectivity, high CO conversion in one pass, stable activity and the possibility of reducing the catalyst for synthesis according to the Fischer-Tropsch method.

In an autothermal reforming process, for example one used in the described apparatus, a combination of partial oxidation and adiabatic steam reforming is used according to the present invention. The product gas is in chemical equilibrium at the temperature at the outlet of the reactor, which is determined by the temperature at the entrance to the reactor and an increase in the adiabatic temperature. The present method is carried out in a fixed bed reactor. Autothermal reforming requires less equipment than conventional steam reforming, and it is a flexible method capable of producing synthesis gas having a composition that varies depending on the regulation of operating conditions.

To obtain synthesis gas from natural gas supplied to the unit, even other variants of the reforming method can be used, for example, reforming in the vapor phase, combined reforming consisting of steam reforming and subsequent autothermal reforming, combined reforming with preliminary reforming, partial oxidation, reforming with gas heating consisting in autothermal reforming and subsequent steam reforming. Other options may be combined autothermal reforming or reforming in the Kellogg system, consisting of a reforming unit and a heat exchanger.

Reactor with distillation (cap) column with catalyst suspension

Among the reactors of the three-phase system used in Fischer Tropsch ground installations, mention should be made of reactors with mechanical mixing of a suspension of catalyst and raw materials, reactors with a loop and reactors with a distillation column with a catalyst suspension. All of them use small particles of catalyst dispersed in a liquid. Thus, for most applications, the liquid must be separated from the suspension to remove liquid products or for the purpose of catalyst regeneration.

The operation of reactors with a distillation column with a catalyst suspension is simple, since there are no mechanically movable elements. Therefore, due to the low diffusion resistance and efficient heat transfer, these reactors are attractive for many industrial processes. However, the separation of solid particles and liquids is usually carried out outside the reactor in complex filter and sedimentation systems. The suspension of the catalyst must be recycled to the reactor, and for this sometimes a pump for suspension is used. Thus, during continuous operation of the reactors with a distillation column with a catalyst suspension, serious problems can arise.

A report recently released by the U.S. Department of Energy dealt with catalyst / paraffin separation in Fischer Tropsch catalyst slurry systems. The report concluded that internal filters immersed in a suspension in a reactor, as used in some experimental or experimental installations, are ineffective due to difficulties in operation. For an experimental setup, a reactor can be used in which part of its wall acts as a filter, however, this is not feasible for industrial reactors. Internal filters are at risk of clogging, which can lead to premature shutdown, and industrial installations are not allowed to seize the opportunity.

The report also indicated that an internal filter inside the reactor suspension was used in a research project. However, although the filtrate flow was initially possible due to the use of a pressure differential, the filter soon became clogged, therefore, it was concluded that continuous operation was not possible, and that for operation on an industrial scale, the separation of solid particles and liquid was necessary outside the reactor.

However, a catalyst slurry distillation column reactor recently developed by the present applicants as described in PCT / NO 94/00023, showed that, in contrast to this known technical solution, a continuous Fischer-Tropsch synthesis reaction system can be created in which does not need to separate solids / liquids in an external filter device, and in which a high filtrate speed can be achieved.

A catalyst slurry distillation column reactor for such a continuous Fischer-Tropsch synthesis reaction system that is well suited for use in the apparatus of the present invention is a reactor in which a liquid product is separated from a phase of a catalyst suspension containing a finely divided catalyst in a liquid medium moreover, said reactor comprises a vessel forming a reaction zone for containing a phase of a catalyst suspension and a volume of gas above the catalysis phase the suspension, means for introducing synthesis gas in the phase of the catalyst suspension into the lower part of the vessel, a filter section for separating the liquid product from the phase of the catalyst suspension, comprising a housing that surrounds at least partially a vessel, a filter element, which together with the housing forms a filtrate zone having an outlet for product filtrate, the filter element being positioned to be in contact with the suspension in the catalyst suspension zone, means for establishing fluid communication between the filtrate zone and that part of the reaction zone, which during application should be filled with a volume of gas above the phase of the catalyst suspension, and a means of establishing an average pressure drop through the filter element.

It was found that the communication between the filtrate zone and the reaction zone, which is achieved due to the aforementioned reactor design, prevents the formation of solid material on the filter element. We believe that this mechanism is as follows. The turbulent movement of the catalyst suspension, when gas bubbles pass up through it, causes a pressure fluctuation on the filter element. A fluid communication between the reaction zone and the filtrate zone simplifies or increases these pressure fluctuations. Therefore, such a system is relatively simple and efficient. The separation stage, which is considered particularly problematic, is achieved without undesirable complications, and under appropriate operating conditions, the filter element is self-cleaning.

Important advantages achieved with such a catalyst slurry distillation column reactor over a fixed-bed multitube reactor are, for example, the following.

Improved temperature control of the Fischer-Tropsch exothermic reaction can be achieved through the use of efficient heat exchangers that are integral with the reactor. Improved temperature control allows high catalyst and reactor performance. The reactor is compact and simple with several elements inside the reactor. The cost of installing a reactor is 5070% lower than the cost of installing fixed-bed reactors (multi-tube fixed-bed reactors).

Internal separation of the catalyst from the synthesis product is carried out according to the Fischer-Tropsch method, which eliminates the need for equipment for external separation of the catalyst.

Since the catalyst is suspended in suspension in the reactor, it is possible to continuously replace the catalyst during operation. Since the reactor contains a suspension of small catalyst particles, it is well suited for the use of highly active catalysts.

Equally important is the high flexibility demonstrated by a distillation (cap) column reactor with a catalyst slurry in terms of operating temperature, product composition, and operating conditions.

In a reactor with a distillation column with a catalyst suspension, the linear gas velocity, catalyst concentration and temperature can be changed without any major operational problems. Thus, you can change the quantity produced and the conversion in one go. In a fixed-bed multi-tube reactor, however, it is necessary to maintain a very high linear velocity in order to achieve favorable heat transfer between the fixed catalyst bed and the reactor wall. Thus, the degree of conversion and the quantity produced cannot be changed to any large degree.

In a distillation column reactor and catalyst slurry, the product composition (paraffin-to-liquid ratio) can be changed over a wide range by changing the temperature of the reactor. This cannot be done in a multi-tube reactor with a fixed catalyst bed, since the reaction rate (for a given catalyst) is determined by thermal equilibrium. Therefore, a multi-tube reactor with a fixed catalyst bed can only be used mainly in the range of low temperatures, for example, 180 - 220 ° C, that is, in the range that gives a high ratio of paraffin to liquid. Indeed, even for a reactor with a distillation column and a catalyst mixture, the reaction rate per unit working volume of the reactor is determined by thermal equilibrium, but in this case, constant heat production can be maintained by simultaneously changing the concentration of the catalyst.

A distillation column reactor and catalyst slurry will be more durable than a fixed-bed multi-tube reactor in unforeseen situations during operation, for example, when the supply of natural gas to the gas synthesis plant is completely cut off. This will not create big problems for a distillation column reactor and catalyst suspension, since the liquid phase that is present in the distillation column reactor and catalyst suspension has a very high heat capacity and, therefore, it will effectively eliminate temperature fluctuations and also other possible irregularities in work. Therefore, a fixed-bed multi-tube reactor must be purged with an inert gas to prevent damage to the catalyst due to excessive temperature. When the unit is restarted, the catalyst in the reactor with a distillation column and catalyst slurry will simply be in a suspended state again when the synthesis gas supply starts, whereas for a multi-tube reactor with a fixed catalyst bed, a more complicated start-up process will be required to eliminate uncontrolled temperature increase.

FIG. 2 shows schematically a corresponding embodiment of a distillation column reactor and catalyst slurry 11 including a reactor vessel 12 and a filtering section 13. Vessel 1 2 typically includes a tubular section 14, and above it a portion 15 in the shape of an inverted cone. The tubular section 1 to 4 forms a zone 20 for the catalyst suspension, which contains a suspension of finely divided catalysts in a liquid medium, for example, from the hydrocarbons of the product. The cone-shaped part 1 5 acts as an expansion chamber to prevent foaming in the suspension and forms a gas cavity 16 above the reaction zone. The cone-shaped portion 15 may contain additional means (not shown in the drawing) to eliminate or reduce foaming.

At the bottom of the vessel 12 there is a gas inlet 17 and a gas distributor 18, through which gas can be introduced into the zone of the catalyst suspension. At the top of the vessel 12 there is a gas outlet 19 for gas from the gas cavity 16. Inside the vessel 12 there is a series of heat transfer pipes 21 extending between the common inlet 22 and the common outlet 23 for the heat exchange medium. The reactor 11 will be controlled by a large number of sensors, regulator valves, pumps, etc., one of which (pressure sensor or temperature sensor) is shown, for example, under 24.

The filtering section 13 comprises an annular body 25, which surrounds the vessel 12 immediately below the cone-shaped part 15. Inside the body 25, a part of the vessel wall is made of sintered metal and, therefore, it forms a filter element 26. The non-porous parts 27 of the vessel wall protrude into the body 25 above and below. corps. The body 25 and the vessel wall effectively form the filtrate zone 28, and above it a gas cavity 29.

An outlet from the filtrate zone 28 serves as a constant level fixture for the filtrate. A pipe 31 protrudes upward from an outlet 32 near the bottom of the housing 25. A horizontal connecting section 33 defines the level 34 of the filtrate in the zone of the filtrate 28 and protrudes downward to the outlet valve 35. The valve 35 opens to discharge the accumulated liquid product in the lower branch of the pipeline. The lower branch, of course, can be replaced by a reservoir for storing a liquid product. The exhaust pipe 31 is filled with liquid product between the hole 32 and the horizontal section 33.

A connecting pipe 38 connects the two gas cavities 16 and 29. The pipe 38 has a valve 39. A pipe 30 is also connected to the pipe 31, which provides fluid communication between the gas cavities 16, 29 and the exhaust pipe 31. The housing 25 also has an inlet 36 near its upper parts with valve 37.

During operation, 8 gaseous reactants are introduced through a gas distributor into the catalyst suspension, supporting the catalyst particles in suspension. Various sensors, such as a sensor 24, and a heat transfer system 21, 22, 23 maintain an accurate reaction temperature. The liquid product is filtered during its passage through the filter element 26 into the filtrate zone 28. This is stimulated by the pressure drop through the filter element caused by hydrostatic pressure as a result of the difference in level between the catalyst suspension and the filtrate. The level 34 is kept constant due to the vertical position of the horizontal section 33 of the exhaust pipe 31.

The turbulent movement of the suspension helps to prevent the formation of a filter cake and to prevent clogging of the filter element 26 by catalyst particles caused by pressure fluctuations through the filter element 26, where the valve 39 remains open.

Gaseous products and any unreacted reagent gases are removed through the outlet 19. Any accumulation of gas above the filtrate in the cavity 29 is eliminated due to the presence of the communication pipe 38.

The filtering section 1 to 3 can be cleaned with a suitable gas, for example synthesis gas, or a suitable liquid, for example a purified product, by opening valve 37 and closing valves 35 and 39. This causes the cleaning fluid to pass back through the filter element 26.

During normal operation, part of the catalyst will be removed and replaced with a new or regenerated catalyst. For reasons of clarity, a device intended for this purpose is not shown in FIG. 2, although it should be understood that any standard system can be used.

A vessel surrounds the reactor vessel at the periphery, preferably at least in part of the length of the reactor vessel. As shown in FIG. 2, the filter element may be formed by a part of the wall of the reactor vessel, which consists of filter material. Alternatively, the filter element is located outside the vessel, and the vessel is interrupted in the area of the filter element. In another embodiment, the filter element is located inside the vessel, and the housing is formed by part of the vessel wall. Preferably, a fluid communication is established between the volume of gas above the phase of the catalyst suspension and the volume above the filtrate.

The communication between the space above the catalyst suspension in the reaction zone and the space above the filtrate in the filtrate zone prevents the formation of pressure drops in excess of those corresponding to hydrostatic pressure. Communication can be achieved respectively through a pipeline passing between the upper part of the reaction zone and the upper part of the filtrate zone and opening into each. Preferably, the pipeline connecting both volumes of gas is intended to facilitate the release of any gas accumulating in the upper part of the filtrate zone.

Preferably, the amplitude or magnitude of the deviations or fluctuations in the pressure drop across the filter element is approximately the same or exceeds the average value of the static pressure drop. It is preferable to maintain the average pressure drop across the filter element at a sufficiently low level, usually less than 6 megabars (600 Pa). If the average pressure drop is below a critical value (for example, 6 megabars), the filter will self-clean.

The value of the pressure fluctuation may be of the order of the differential pressure, for example, from 10 to 200% of the differential pressure. The true value of the pressure drop can be from 1 to 100 megabars, preferably 2-50 megabars.

The means for introducing gaseous reactants or components may contain any suitable means, for example, a cap plate, a plurality of nozzles, a plate of sintered glass melt and the like, preferably located at the bottom of the reaction vessel.

A more detailed description of a distillation column reactor and catalyst slurry is given in PCT International Patent Application No. 94/00023, which is incorporated herein by reference. Reference is also made to PCT / ΝΘ 93/00030 and PCT / ΝΘ 093/00031 and UK application AI 9317605.

Installation of a system on a floating vessel for oil production, storage and unloading The method according to the present invention is particularly suitable for use in an installation located on board the so-called FPSO vessel (FPSO - floating vessel for production, storage and unloading), which may be a vessel , built and equipped with equipment for loading / unloading hydrocarbons in the offshore oil field and from wells for gas production, for storing such hydrocarbons and production, especially for the conversion and upgrading of hydrocarbons, x from the wells.

Vessels of the mentioned type were shown and described by the present applicants in a number of patents and patent applications, which they called the MST vessels (MST - multipurpose shuttle tanker). A vessel of this type is particularly well suited as a cargo vessel for an installation designed to carry out the method according to the present invention, and it will allow to use to the highest possible extent the potential for flexibility and integration of such an installation.

A vessel of the type mentioned is shown schematically in FIG. 3, which is a side view. At the fore end of the vessel there is an immersed receiving cavity 40, open downward for receiving an underwater buoy 41 and a service shaft 42, which extends between the receiving cavity 40 and the deck 43 of the vessel. The device is designed in such a way that the submerged buoy for loading or unloading hydrocarbons can be pulled up and fixed in the receiving cavity, as described and shown in more detail in International patent applications PCT / NO 92/00053, PCT / NO 92/00054 and

PCT / NO 92/00055, and it is also possible to pull up and fasten the buoy, which is designed to interact with the swivel mechanism located at the lower end of the shaft, to use the vessel as a production vessel, as described and shown in more detail in European patent applications No. 93913638 and Norwegian Patents Nos. 922043 and 922045. A link to the mentioned applications is given here to describe current options.

As you can see, the wheelhouse 44 of the vessel is located near the bow 45 of the vessel, and further, under the wheelhouse engine room 46 with its diesel and electric main machinery. The service shaft 42, which is located between the buoy 41 and the deck 43 of the vessel, is located just behind the wheelhouse, so the team that is to descend into the shaft will be on the leeward side behind the wheelhouse.

It is shown that a loading pipeline or swivel 47 is located above the buoy for connection with the buoy, as well as a connecting pipe with a valve 48 of the oil pipeline. The following shows control means 49, for example, television cameras, a shutter 50 for closing the shaft 42 above the receiving cavity and guiding means 51 for use in conjunction with pulling up the buoy. It is also shown that on the deck there is a winch 52 for pulling, a pantry 53 and a crane 54 for use in connection with, for example, repair. In the bow of the vessel is a pair of bow propellers 45.

Technological equipment for oil processing is installed on runners on the deck between the front and rear of the vessel. The flow of oil from the well, which is produced in the oil field and rises up to the vessel through vertical pipes from the oil field and subsea buoy 41, is divided here into water, oil and gas. This equipment is shown in the form of a plurality of portable modules 56. Between the front and rear of the vessel there are many cargo compartments or tanks 58. It is shown that a hanging boom 57 is located at the rear.

FIG. 4 is a perspective view of a production vessel carrying an apparatus according to the present invention for converting bound natural gas to synthetic crude oil and / or paraffin. The installation is located behind the wheelhouse 65 in the bow of the vessel and behind any present receiving cavity (not shown) for receiving an underwater loading buoy.

Positions 1, 2 and 3 show the same process equipment as in FIG. 1, i.e., an absorption unit 1, in which sulfur is removed from natural gas, a synthesis gas reactor 2, consisting of an autothermal reforming unit, and two reactors 3 with rectification (cap) columns and with a catalyst suspension for performing synthesis according to the Fisher method -Tropsha. The installation for the extraction of hydrogen from a part of the synthesis gas is indicated at 66, and the installation for the extraction of oxygen for supply to the autothermal reactor is indicated at 67. Technological equipment 1, 2, 3, 66 and 67, as well as other equipment connected directly to the installation (it is assumed in this drawing, without specifying any specific position) are mounted on standardized replaceable structures with skids 68 attached to the deck of the vessel. These skid designs can be easily removed to free the ship deck for other uses.

An important aspect of the preferred embodiment of the system according to the present invention is that the system is fully adapted and integrated with the technology forming the basis of the multi-purpose shuttle tanker, which will preferably carry the installation. This means that the design of the system is adapted to the dimensions of the skeleton for installing the modules, that is, it is adapted to the infrastructure of the production vessel, including, for example, the central pipe rack, and it is adapted to various auxiliary systems that supply cooling water, steam, oxygen, etc. .P. The system must also be adapted thoroughly and optimally for oil production in any particular case, in particular, to the amount of associated gas produced and the degree of gas injection. The advantage achieved by integrating the installation with auxiliary systems on board the production vessel is, for example, that the unconverted gas from the installation can be used to generate electricity in an electric generator or to produce fresh water from sea water. An advantage is that a relatively large amount of water, which is separated from the product from the Fischer-Tropsch reactors, and which contains acid (e.g., acetic acid) and alcohol (e.g., methanol), can be used for injection purposes in the field. An added benefit is the easily accessible seawater for cooling purposes.

The installation according to the present invention will have a capacity in the range of 420 - 21000 barrels of C ₅ / day (53.5 - 2675 t C ₅ / day), corresponding to the supply of natural gas 0.1 - 5.0 million st.m ³ / day, preferably production in the range of 2100 - 8400 barrels of C5 / day (267.5 - 1070 tons of C5 / day), corresponding to the supply of 0.5 - 2.0 million st.m ^{3 of} natural gas per day. The size of a particular installation will correspond to a capacity of approximately 4,200 barrels of C5 / day (approximately 535 tons of C ₅ / day), corresponding to approximately 1.0 million st. m ³ natural gas per day.

Synthetic crude oil and / or paraffin obtained as a product from the unit can be mixed with crude oil produced from a well (s) and thus transported with it. Or the product from the installation can be sent to separate tanks for the product for separate unloading from the production vessel and for sale or its cleaning. In many cases, this can be beneficial, since the product obtained from the synthesis gas formed in the installation will usually surpass conventional crude oil in quality and properties, since it contains practically no sulfur. Thus, it can be suitable, for example, as a starting material for producing diesel fuel with a high content of cetane and high-quality components of lubricating oils.

An additional advantage of the skid mounted installation is that it can be mounted on appropriate ground means for the production of synthetic crude oil during periods when it is not used on board a production vessel.

Such installations, which are not suitable for a multi-purpose shuttle tanker, can be used on ships intended for these purposes, on fixed offshore installations, or in places on the coast where, for example, gas at a remote distance may be of interest as a feedstock for the installation.

The following describes, as an example of operation, a simulated version of a portion of the Fischer-Tropsch method according to the present invention used in the apparatus as shown in FIG. 2 and described generally above.

Working example

Using a mathematical modeling model for reactors with a distillation (cap) column and catalyst suspension developed by the present applicants and based on the reaction kinetics for the catalyst described below and confirmed correlations for mass transfer and hydrodynamics in distillation columns with a catalyst suspension, data were obtained for the operation of the part Fischer-Tropsch apparatus according to the present invention, as shown in FIG. 2, containing two reactors with a distillation column with a catalyst suspension, connected in series with the removal of condensed water and C ₅ + between the reactors, to obtain liquid hydrocarbons (C ₅ +) from the synthesis gas.

A cobalt-rhenium catalyst containing 20% by mass of Co and 1% by mass of Re, supported at γ-Ά1 ₂ Θ ₃ , was used in the reactors. The catalyst described in US patent No. 4801573, prepared by impregnation

Y-A1 ₂ O ₃ aqueous solution of Co (NO ₃ ) ₂ -6H ₂ G and HReO ₄ , according to the method of rudimentary wetting.

The synthesis gas of the composition shown in Table 1 below was introduced into the first of two series-connected reactors (reactor 1) in an amount of about 153,000 std.m ³ / h. The supplied amount of synthesis gas corresponds to about 1 million stdm ^{3 of} natural gas supplied to the reforming section of the installation plus recycled synthesis gas from reactor 2 with a distillation column with a catalyst suspension. The composition of the synthesis gas is typical of the synthesis gas obtained from the remote gas.

The operating conditions and basic data for the two reactors 1 and 2 are presented below in table 2.

The various mass flows to and from Reactors 1 and 2 are shown in Table 3. It was found that the total percentage of CO conversion in two reactors in one pass was 89%.

Table 1. The composition of the synthesis gas supplied to the reactor 1

Component Molar% H2 58.3 BUT 0.3 With 29.0 CO2 11.6 N2 0.5 CH4 0.3

table 2

Reactor 1 Reactor 2 Height (m) ¹ ) 10 10 Diameter (m) 5.8 3.9 Linear gas velocity (m / s) ² ) 0.1 0.1 Reactor temperature (° C) ³⁾ 230 230 Total pressure (bar) thirty 28 The concentration of catalyst (wt.%) twenty twenty Conversion (CO) (%) 66.5 67.0 Reactor capacity (kg HC / m ^s / h) 70 fifty Catalyst productivity (kg HC / kg catalyst / h) 0.50 0.37 Selectivity for C ₅ + (%) ⁴⁾ 88 87

¹ ) The height of the loosened catalyst suspension ²⁾ At the inlet ^{3) The} average value

4)

The number of moles of CO, converted into C ₅ +

The total number of moles converted WITH

Table 3. Mass flows (t / h)

Component Reactor 1 Reactor 2 in of in of H2 8.0 2.6 2.6 0.8 H2O 0.3 23.5 - 7.7 With 55,4 18.5 18.5 6.1 CO2 35.0 35.6 35.6 36.0 N2 0.9 0.9 0.9 0.9 CH4 0.3 1.3 1.3 1.7 C2-C4 - 1,2 1,2 1,6 C5 + - 16.3 - 5.3

CLAIM

Claims (7)

CLAIM 1. Method for carrying out in the open sea, on a ship, platform or other installation for converting natural gas, in particular associated natural gas, into synthetic crude oil and / or paraffin in two stages, in which (1) natural gas is converted into synthesis gas consisting of a mixture of carbon monoxide, hydrogen and carbon dioxide in an installation for producing synthesis gas, and (2) the synthesis gas is converted into synthetic crude oil and / or paraffin during Fischer-Tropsch synthesis, characterized in that the synthesis gas stage (1) for the implementation of the synthesis of p The Fischer-Tropsch method is introduced into a suspension consisting of liquid products, fine particles of catalyst and synthesis gas, into a reaction zone in a reactor with a distillation column with a catalyst suspension, in which the internal separation of liquid products from the rest of the catalyst suspension is carried out. 2. The method according to p. 1, characterized in that the synthesis gas from step (1) after cooling and separating water is introduced into the lower part of the reaction zone in a reactor with a distillation column with a catalyst suspension, and the reaction zone is located so as to take a catalyst suspension consisting of liquid products, finely divided catalyst particles and applied synthesis gas, and a volume of gas above the catalyst slurry phase, the liquid product is separated from the rest of the catalyst slurry using a filter section, including In the housing and filter element, which together form a filtrate zone, having an outlet for the product filtrate, the filter element is in contact with the catalyst slurry in the reaction zone; a fluid communication is established between the filtrate zone and the part of the reaction zone containing the volume of gas above the catalyst slurry, and the average pressure drop is established through the filter element. 3. The method according to claim 1 or 2, characterized in that the conversion of natural gas into synthesis gas at the stage (1) is carried out by means of partial oxidation. 4. A system for converting natural gas, in particular bound natural gas, into synthetic crude oil and / or paraffin in two stages, in which (1) natural gas is converted into synthesis gas consisting of a mixture of carbon monoxide, hydrogen and carbon dioxide, in an installation for producing synthesis gas, and (2) the synthesis gas from the installation is converted into synthetic crude oil and / or paraffin in a Fischer-Tropsch installation, characterized in that the Fisher-Tropsch installation contains one or more distillation column reactors with a catalyst suspension Each one contains a reaction zone designed to contain a catalyst slurry consisting of liquid products, finely divided catalyst particles and synthesis gas, and the reactor (s) is intended for the internal separation of liquid products from the rest of the catalyst slurry. 5. The system according to claim 4, characterized in that each reactor with a distillation column with a catalyst suspension contains a vessel forming a reaction zone designed to contain the phase of the catalyst suspension and the volume of gas above the phase of the catalyst suspension, the means of introducing synthesis gas into the phase of the catalyst suspension in the lower zone of the vessel, a filter section designed to separate the liquid products from the catalyst slurry phase, comprising a housing that surrounds the vessel, at least partially, and filtered An element that together with the said housing forms a filtrate zone having an outlet for the product filtrate, the filter element being arranged so as to be in contact with the catalyst slurry in the catalyst slurry zone, means establishing a fluid communication between the filtrate zone and that part of the reaction zone, which during the application must deal with the volume of gas above the phase of the catalyst suspension, and means for establishing the average pressure drop through the filter element. 6. The system according to claim 5, characterized in that it is installed on the runners, which can be easily attached with the possibility of replacing them on the vessel, sea platform or other installation located in the open sea. 7. The system according to claim 6, characterized in that it is adapted for installation on a vessel intended for the extraction, storage and unloading of oil in a floating state