TW201006919A - Improvements in or relating to processing associated gas - Google Patents

Abstract

A plant is provided for processing natural gas. The plant comprises two or more modules connected in parallel. The plant is configured to convert the associated gas into a material with a higher density. In addition, a method of processing gas associated with one or more oil wells. The method comprises the steps of: providing a modular plant comprising two or more modules in parallel wherein at least one of the modules is a robust module and at least one of the modules is an economical module; turning down one or more of the modules when productivity drops; switching off one or more of the modules at least when productivity drops beyond the turndown limit.

Description

201006919 IX. INSTRUCTIONS: TECHNICAL FIELD OF THE INVENTION The present invention comprises a solution for treating associated gases. As such, the invention comprises a "syncrude" for the manufacture of synthetic crude oil. In particular, the invention encompasses a process for the manufacture of synthetic crude oil from associated gases. Furthermore, the present invention relates to a GTL apparatus for treating associated gases, particularly for converting associated or standard gases into synthetic crude oil. © [Prior Art] The associated gas is natural gas found with crude oil, which is soluble in the free gas cap above the oil. Associated gases are by-products of refining, and the secondary • associated gas disposal options that must be disposed of in the absence of means to capture and transport them can cost more than US$100 million without the economic benefits. As a result, most of the gas is conventionally burned off. However, the increasingly stringent environmental regulations are increasingly unable to burn from a political and environmental perspective. In particular, gas combustion contributes to carbon monoxide, nitrous oxide and methane emissions, and is a source of noise and unwanted heat and light, affecting nearby communities and surrounding plants. In any case, the consumable resources are discarded and the pumping plant operates inefficiently without generating revenue from the associated gas. Individual studies have estimated that 'the global associated gas has no commercial price due to its lack of capacity of 1,000 trillion cubic feet (tcf) and is accompanied by millions of barrels of oil. In 2003, the World Bank reported a global burnout of 4.: gas. It is equal to the combined annual consumption of France and Germany, or 25% of the US consumption. In addition, the world recharges 12.5 tcf of gas. It is estimated that the other state of the device and the achievement, more modular or as many products. Providing straight and accompaniment to the burning, and the use of the surrounding technology is more than! The gas of 700 5 tcf eliminates 50% of the 201006919 represents a worrying recharge; or the gas is recharged due to lack of feasible or economic alternatives . One option for treating associated gases is to recharge the extracted gas back into the field. However, it requires gas purification and compression, which creates additional costs in manufacturing that increase with reservoir pressure differentials. In addition, the recirculated gas may actually damage the oil production by negatively affecting its flow. An alternative is to find ways to make the associated gas on the market. Technically, there are several options for gas utilization: it can be prepared into various forms of fuel (anhydrous ® pipeline natural gas, LPGs, LNG, or gas wiring - local power generation) or treated for petrochemical feedstock. Other options currently under development include Gas-T liquid KGTL and Gas to Solid (GTS). GTL technology offers a wide range of end products that are superior to conventional petrochemical alternatives such as clean wood • oil and jet fuel, middle distillates, lubricants, olefins, and methanol. GTS - is a fairly novel technology developed specifically for marine natural gas, in which natural gas is converted to hydrates for easy transportation and regasification at the receiving end. ® However, the treatment of associated gases is still not profitable and depends on the gas itself or the existing market for gas derived products. In particular, oil companies regard the light hydrocarbons of large fractions (the basic components of the petrochemical industry) as the most promising use of associated gases. Another disadvantage in considering the solution of associated gases is the enormous expense of transporting the gas to the consumer area. Long-distance pipelines and LNG尙 have not become conventional gas delivery methods, although they are highly feasible in some cases. The pipeline or conversion to LNG is also preset to a specific amount of associated gas from the well to make this delivery and treatment economically feasible. Therefore, exhaust gas or combustion is the least expensive method. Other considerations 201006919 is that it must be included in the health and safety aspects of the device when handling combustible gases, and if the gas is too acidic (collecting high levels of H2s) or has high Equipment handling and maintenance of liquid content. As a result, oil companies have a clear, sustained need to translate this responsibility and cost into assets that generate positive economic profits. One of the main problems in dealing with associated gases is the change in production rate, so the life of the field can be treated with the accompanying gas regardless of the volume of the accompanying gas. Conventional gas-liquid (GTL) plants are typically configured for onshore applications and can economically develop large quantities of natural gas fields (25,000+ barrels per day). This device typically costs billions of dollars and requires a large area and is cumbersome. In fact, the larger the device, the better the economic output of the device. These units typically use a fixed bed or stream, and a bed-bed slurry type reactor converts natural gas into refined products such as waxes and lubricants. It should be understood that the device is not suitable for the marine position due to at least its size and weight. As shown in Fig. 1, a schematic diagram showing the variation of the output or flow velocity V with time T shows that the gas supply R required for the conventional GTL is substantially fixed. Conversely, gas productivity G, the flow rate of associated gas from the field (measured as bbl/day or cubic meter/曰), varies with the operational life of the field, and the life of the field typically ranges from 3 to 20 years. During the initial period, productivity G increased the most, which was a plateau with a substantially fixed productivity, and then productivity declined. Short periods of productivity (such as days or weeks) may fluctuate randomly, typically about 10% of their average. For example, if the well undergoes an emergency shutdown, it will cause very short-term changes. In this scenario, the flow of the well falls within a few minutes from 201006919 to zero. In general, it may be equivalent to a 20% reduction in flow rate for several wells. If the oil facility itself is shut down urgently, it will fall to zero in a few minutes or less. Although the conventional refinery-scale GTL unit has the ability to adapt to each move, the unit is configured to be fully loaded with long-term capability and the power is reduced from full load to almost zero. When large devices are scaled down, they are no longer commercially viable. Referring to Figure 1, it should be understood that for gas, this conventional device is only for the early to mid-term of the oilfield life. Is it economical to include GTL facilities in the oil pumping plant?

In order to break into the oil plant, the GTL facility is highly desirable to adapt to changes in oilfield productivity, especially when productivity is reduced. In order to change over time, modular systems are ideal - modules should be commercially stable when operated separately, allowing GTL, production to scale up and combine several modules, and productivity as a single module. It has proposed a two-stage process to treat the GTL of natural gas to form syngas, and the second stage to use the snow-synthesis method to form a gas that can be regenerated by steam/methane recombination (SMR) or by natural gas. It has developed micro and mini channel technology for SMR and [reactors], especially modularization. However, there is still a continuing need for improved technology in the sector. It has developed a new generation of syngas production means using natural gas from membranes (ITMs). ITMs are non-porous ceramic membranes that can simultaneously diffuse. The gas produced in the oil production facility is generated by the productivity wave. The production will not cause the installation to be associated with the treatment. Therefore, the problem arises. GTL facilities can be answered with the life of the field. The facilities are reduced at the peak and the dismantling method. The first stage is hydrocarbon. Synthetic Partial Oxidation Shouxue Snow-阙 Synthetic and Economical Manufacturing Syngas Oxygen Ion and Electricity 201006919 The reactor for converting natural gas to syngas using ITMs is operated using two input streams, the first input stream being a combination of natural gas and steam. And the second input stream is air. These streams contact the opposite surface of the ITMs. It reacts on the surface of the combined natural gas and vapor combination: CH4 + Ο 2' ^ CO + 2H2 + 2e' On the opposite surface of the ITM, it ionizes oxygen from the air and oxygen ions pass through the membrane.

Vi 〇2 + 2e' Ο2' ® Hydrogen and carbon monoxide can be used to make synthetic crude oil by snow hydrazine synthesis. The synthetic crude oil can then be mixed with the oil associated with the liquefied natural gas. As a result, no additional transportation costs occur when the synthetic crude oil is transported with the oil. However, the conventional device of the Fisher-阙 synthesis method is quite different from the small device that uses ITMs to produce syngas. • SUMMARY OF THE INVENTION Accordingly, the present invention has been made in view of the background. In particular, it has been considered to provide a complete economic answer to the associated gas problem, and to configure a GTL device that can overcome the cost, size, and inelasticity of conventional GTL devices. In particular, it should be understood that the associated gas market requires scalability, elastic output, and it must be suitable for marine and onshore operations. The present invention therefore broadly encompasses an improved, modular, compact GTL device. The present invention provides an answer to an associated gas. In particular, the present invention is a device for extracting crude oil and associated gas from an oil field, wherein the associated gas is converted from a gas to a synthetic crude oil "syncrude", and optionally the synthetic crude oil is intermixed with the extraction oil. -10-201006919 In another aspect, the invention is a gas-liquid (GTL) unit integrated into a pumping unit where the GTL unit converts the gas to synthetic crude oil and optionally blends the synthetic crude oil with the crude oil. The intermixed crude oil can then be stored and transported together for downstream processing and refining. In these aspects, the composition of the synthetic crude oil can be adjusted in a modular manner to substantially conform to the composition of the crude oil extracted from the oil field. Further in accordance with the present invention there is provided a GTL apparatus for treating associated gases wherein the apparatus comprises at least one small synthesis gas reactor and at least one small Fisher-Symmetric synthesis reactor. In a further embodiment, two or more syngas reactors may be coupled together. Additionally or in an alternative embodiment, two or more smaller Fisher-Shrimp synthesis reactors can be connected in parallel. Each of the small Fishers _ ' 阙 synthesis reactors comprises a reactor zone defining a plurality of channels for the Fisher-阙 synthesis reaction, each of which contains a removable metal support with a catalytically active material. In a further embodiment, the two Fisher-Sylon reactors can be connected in series. Alternatively or additionally the GTL device may comprise a first set of reactor module stomachs comprising a plurality of identical small Fisher-Symmetric reactors connected in parallel, and a second set of reactor modules comprising a plurality of parallel connections A small Fisher-阙 synthesis reactor, the second group is in a series relationship with the first group. In one example, the or each syngas reactor comprises at least one ceramic membrane separating a channel carrying a methane-containing gas stream and a channel carrying an oxygen-containing gas stream, and wherein the or each ceramic membrane can conduct oxygen ions from the oxygen-containing gas stream Diffusion into the methane-containing gas stream. This membrane can be referred to as an ion transport membrane (ITM). Each of the small syngas reactors may comprise a pressure vessel encasing the ceramic membrane. Each small syngas reactor -11- 201006919 may also contain a recombination catalyst. Where the syngas reactor utilizes a ceramic membrane through which oxygen ions can diffuse, the membrane separates the first stream comprising oxygen from the second stream comprising methane; preferably the second stream also contains vapor. If no vapor is provided, the reaction occurring in the second gas stream is similar to that in the partial oxidation reactor, and if steam is supplied, it is similar to that in the autothermal reforming reactor. The catalyst can be provided on one or both sides of the ceramic membrane. A syngas reactor comprising a multi-layer ceramic sheet is described, for example, in U.S. Patent No. 7,279,027, the entire disclosure of which is incorporated herein by reference. Ideally, it integrates or integrates a GTL device into a pumping plant. "Pumping Plant" means a unit that extracts, treats and stores crude oil from one or more wells. Therefore, the GTL device can be adapted to any location in the oilfield processing and development device. • Preferably, the pumping plant or oil production facility is located near one or more wells and the oil comes from the oil well and the oil is initially disposed of at least prior to storage or transport through the pipeline or other output facility. For example, the device or facility can be a fixed platform or a floating production storage and offloading (FPSO) vessel. In general, this facility connects between 1 and ® 20 separate wells in a single field. Oil plants can also refer to small facilities such as oil well test vessels.

It will be appreciated that by converting the associated gas to synthetic crude oil that is qualitatively compatible with the crude oil extracted from the field, it does not require a specific gas output facility. In addition, no specific GTL process product storage is required and no refining is required. In fact, it foresees the use of existing transportation and installation networks to transport and refine mixed oils with synthetic crude oil. In this way, there is no need for a specialized device for extracting, storing and transporting specific fractions of synthetic crude oil, so that the size, complexity, etc. of the GTL-12-201006919 device can be significantly reduced, thereby improving economics. In particular, if an oil field has been invested, the plant, storage and transportation network is already available. The addition of a GTL unit in accordance with the present invention to an integrated oil pumping plant to treat associated gases provides additional benefits. For example, any gas other than the associated gas found in the oil field may be extracted, thereby increasing the output and profit of the oil field. In other words, the invention has the potential to increase the economic output of the field. In some cases, it also extends the life of the field, not only because it does not jeopardize oil or flow due to reinjection, but also because it provides an option for additional benefits from non-associated gases. The GTL unit can be any small GTL unit as long as it can be integrated or integrated with the pumping station. In particular, the GTL unit may comprise at least one vapor/methane recombination (SMR) reactor and at least one reactor for performing Fisher-Fluor (FT) synthesis. The basic difference between the GTL device of the present invention and the state of the art GTL device is the size of the device, and the device does not have to include means for converting synthetic crude oil into a refined product. Typical (non-small) GTL units are the size and scale of refineries, with lengths of up to several miles. Although this device is effective and economically viable for non-associated gases, and can be reduced to the extent of processing large volumes of associated gases, it can be reduced to an extent that is not economically viable. Therefore, the use of a typical GTL device with a limited lifetime of the oil field (especially associated gas) is limited. This GTL unit can be used only for part of the life of the field rather than the full life. It will be appreciated that the apparatus of the present invention can be combined to produce oil producing facilities for associated gases and crude oil. In this particular embodiment, the operation comprises separating the gas from the crude oil, such as a treatment plant using a combined oil/gas separator, for example, from 13 to 201006919, by steam/methane recombination to produce a synthesis gas, and then accepting the synthesis gas. Snow-germanium is synthesized to form longer chain hydrocarbons. The longer chain hydrocarbons can then be combined with the oil, or can be refined into directly marketable products such as waxes, lubricant base oils, paraffins, and oleins. The overall result is the conversion of methane to higher molecular weight hydrocarbons, which are usually It is a liquid under ambient conditions. The two stages of this process (steam/methane recombination and Fisher's synthesis) require different catalysts and therefore different catalytic reactors. As the reactions are each endothermic and exothermic, the catalytic reactor transfers heat back and forth to the beta reaction gas; the heat required for vapor/methane recombination can be provided by methane combustion. The advantage of using a small or microreactor is that the ability to use the apparatus of the reactor can be easily changed to accommodate changes in gas supply, such as with oilfield life, changes in life supply, oil well closures for days and weeks, or even seconds, Short-term supply fluctuations of minutes or hours. In addition, the device can more easily conform to the gas profile, as the small scale reactor provides for the configuration and construction of the device in a more resilient manner. It is the opposite of a typical GTL device, where the gas volume curve is typically matched to the device because the device configuration and requirements provide less flexibility. The present invention also provides a processing apparatus for treating an associated gas, the apparatus comprising a separator for separating a gas and an oil, and a gas processing apparatus incorporating an oil/gas separator for recombining a synthesis gas by steam/methane and A plurality of identical modular recombination reactors connected in parallel, the processing apparatus further comprising a plurality of identical modular synthesis reactors connected in parallel for performing Fisher-Dynamic synthesis, thus producing longer chain hydrocarbons. This apparatus may further comprise means for combining longer chain hydrocarbons with oil. -14- 201006919 Where the associated gas is treated and where the gas is treated in combination with the oil/gas separator, the ability to operate satisfactorily is particularly important despite the rate of production of the associated gas. The present invention also encompasses a A device in which one or more modules in a device are exchanged for substantially the same module, wherein substantially the same module includes a new or repair catalyst. Preferably, the reactor includes a removable catalyst in some or all of the reactor channels. The catalysts in these reactors have a limited lifetime and can be removed and replaced due to the configuration of the reactor, or only repaired. In this way, the reactor, and thus the module, can be reused in its original device or used to replace modules in devices at different locations. The invention also encompasses a module for use in a GTL apparatus of the invention, the mold set comprising at least one syngas reactor, which may be an SMR reactor. In a specific embodiment, the module further comprises at least one FT reactor. The catalyst in the reactor can be new or repairable. It will be appreciated that the invention may be practiced on land or in the ocean. The invention is particularly useful for sea ® ocean production, such as FPSO, where the most important equipment and storage space is maritime transportation and handling. The use of small mini-channels or microchannel reactors allows the GTL unit to be located on the same FPSO as the oil plant, thus reducing the total plant cost of the field. The invention is particularly suitable for gas to oil ratios of between about 35 and 350 cubic meters per cubic meter (about 200 to 2000 scf/bbl, where 1 bbl = 1 barrel = 42 US gallons, and 1 scf = 1 cubic inch at STP) Facilities, although they can be used in facilities with a slightly lower proportion, such as as low as 15 m3/m3. It is in contrast to a non-associated gas GTL device typically produced from a gas field or condensate field having a gas to oil ratio of -15 to 201006919 and greater than 5000 cubic meters per cubic meter. The term "gas to oil ratio" means the ratio of the volume of the associated gas measured in STP to the volume of the oil. Larger gas oils are more cost effective to treat gases in other ways, such as the manufacture of liquefied natural gas. For significantly smaller gas to oil ratios, the economics of this process may be insufficient, and in fact the oil production facility itself may require some natural gas to enhance its own operations. In one aspect, the invention comprises a GTL device wherein the components of the device are modules. In other words, the present invention is a GTL device for treating associated gases, wherein the device comprises one or more module assemblies. In a specific embodiment, the apparatus includes one or more modules, wherein each module includes at least one syngas generating reactor, and at least one Fisher-Fluor (FT) reactor. In another embodiment, the module comprises one or more syngas generating reactors or one or more Fisher-Fluor (FT) reactors. In yet another embodiment, the apparatus includes a plurality of syngas generation reactor modules and a plurality of Fisher-Fluor (FT) reactor modules. Each syngas producing reactor can be an SMR reactor. ® In this way, the GTL device can be constructed to reflect the gas volume curve. In particular, the GTL device can be constructed to accommodate the decreasing gas volume curve. This is in contrast to the current GTL configuration, which has a fixed production capacity and a fixed feed rate. The apparatus of the present invention can increase or decrease the module according to the amount of gas available, thereby adjusting the overall productivity of the GTL device with respect to the availability of gas, and changing the degree of gas production with the life of the field. That is, the number of reactor modules can be adjusted over time to conform to the profile of the associated gas production. In particular, as gas manufacturing declines, individual modules can be turned off only or can be removed from the device. -16- 201006919 In particular, the oil/gas field A may have a gas production force x, and the ?fi has a gas production force 2X. In order to increase capacity, rather than extending the pipeline area, etc., the capability can be increased only by adding modules to the GTL device. It is used in the treatment of associated gases because the minimum level of gas that must be treated is close to zero. The GTL selection allows the associated gas produced in the gas field to be used when the unit is operating at full capacity. Such a GTL device must be able to cope with a 10 to 100% productivity change. The present invention overcomes this burden on β. In order to deal with short-term fluctuations in gas manufacturing, GTL is installed. No, the same reactor can vary depending on the catalyst used and the reaction. The percentage of total down-regulation of GTL devices is limited by the lowest (which may be 50% down). Therefore, the range is from 50% to 100%. The maximum possible down-modulation of the modular device is to turn off only the remaining remaining modules. For example, in a device with 5 individual ® , the productivity range is 10% to 100%. In a modular unit, the total down-regulation can be limited by components of the reactor (such as compressors, preheaters, and gas pretreatment units for mercury removal). The performance of these auxiliary components may be negatively affected by the non-speed. If the reduction in associated gas production is too severe and unreasonable, the process of sufficiently shortening the process to shut down the one or more gas feeds may be at least partially replaced with methanol. The oil/gas field can be larger and provide the required capacity. The capacity of the device is 100% oil / the economical and technical modularity can be used to lower the finite element geometry. Downgrading the productivity of a device with a small tolerance component, and adjusting the module's capacity or assistance by 50%, including desulfurization and a low gas flow module below the module, accompanied by a reactor - 17-201006919 Maintaining the operating temperature allows for the advantage of switching back to the associated gas as quickly as possible when the associated gas production rate is sufficient. In addition to fluctuations and changes in gas volume, another issue in dealing with associated gas considerations is that the composition of the gas changes with the life of the field. If the composition changes, in a device that treats the gas by pre-recombination to provide a standardized gas composition for introducing a syngas to produce a reactor, the composition change results in a volume change. Therefore, the modular device can be easily adjusted to cope with composition changes compared to devices with higher capabilities. © This or each module may contain one or more reactors connected in series, in parallel, or a combination thereof. In fact, the module or modules may comprise two or more reactors connected in series, in parallel, or a combination thereof. For example, an FT module can include several FT reactor zones that are welded together. In another example, the FT module can comprise * two sets of FT reactor zones arranged in series. In this manner, the syngas passes through a zone of the FT-reactor, thereby passing the remaining syngas through the second FT reactor zone. Syngas was previously provided as a partial conversion of synthetic crude oil. The output of the first FT reactor can be subjected to a beta treatment, such as separating the condensable liquid from the output, prior to passing the remaining syngas through the second FT reactor zone. Preferably, the synthesis gas manufacturing system is carried out using a plurality of modular reactors operating in parallel. Similarly, it is preferred if the Fisher-Symmetric synthesis is carried out using a plurality of modular synthesis reactors operating in parallel. In a preferred embodiment, it is envisaged that the reactor constituting the module or modules is a small reactor or a minichannel reactor, such as WO 01/51194 (Accentus pic) or WO 2006/79848 (Compact GTL pic). Said, or a microreactor, as described in U.S. Patent No. 6, 568, 534 (Wang et al., -18-2010, 069, 919) or U.S. Patent No. 6,6, 196 (Tonkovich et al.), the reference. This reactor is ideally configured for modularization because of its full size and weight. In fact, this small reactor is particularly suitable for marine applications, especially since the Fisher-Head reactor does not require the use of a fluidized bed. A further benefit of all methods is that it does not require the provision of a pure oxygen supply. In addition, the reactor can be constructed to an economical unit as small as 200 barrels per day. It is also known that this reactor has a small liquid inventory, which is an important consideration when configuring a marine device, and the reactor that becomes a module can easily be plunged into a floating production storage and offloading (FPS0) ship because of its small size. Or in the production platform. Another important advantage of the present invention is that if a module fails, or the catalyst degrades, the module can be removed and replaced without significantly affecting the overall output of the device, or in fact without having to shut down all of the devices and replacement. In another embodiment, the device may include a "standby" or backup module. If the productivity should increase suddenly or the module fails, it provides additional capabilities. Ideally, the modules are identical and interchangeable. Therefore, it is foreseen that the module is of a standardized size, which can be removed by standard processing equipment and replaced with a similar standard size. Preferably, the module is suitable for the formation of a synthetic gas (for example, by recombination) or for synthesis, and is suitable for the size of an ISO container, and has a weight of not more than about 35 tons, preferably not more than 25 tons, and more preferably. It is no more than 15 tons. As a result, the module can be installed and replaced using stacking equipment for oil platforms and FPS0 ships. If a large number of smaller modules are deployed to process associated gases from a single well or a group of wells, there is an increase in the number of manifolds and valves that connect and control the flow of associated gases and products to the various modules that make up the unit. Therefore, although it is better to -19-201006919 to fully reduce the weight of the module to use the standard container processing module for ISO container stacking, the weight is shown as an example of the weight limitation of these devices, and should not be regarded as a desire to mold The weight of the group is reduced to exceed the limit imposed by the processing equipment. In a particularly preferred embodiment, the apparatus may preferably produce longer chain hydrocarbons of no more than about 800 cubic meters per day (5 000 bbl per day) or no more than 950 cubic meters per day (6000 bbl per day) ( For example, the optimum scale of C5+) is gas treatment, synthesis gas formation and synthesis (including Fisher-阙 synthesis). It corresponds to a gas treatment of no more than about 2.0 x 106 cubic meters per day (70 Mscf / day) or 2.5 x 10 6 cubic meters / day (85 Mscf / day) (although the gas corresponding amount depends on the processing device (including gas processing, recombination and synthesis devices) ) depending on the degree of integration between other operations of the thief equipment). This unit can be adapted to a well's platform or FPS0 ship. - In another aspect, the present invention provides a method for operating an oil producing facility that produces associated gas with oil, wherein the method involves separating the gas from the oil, using a treatment unit incorporating the oil/gas separator to borrow steam/methane Recombination treatment of W gas to produce synthesis gas, synthesis gas acceptance of Fisher-Synthesis to form longer chain hydrocarbons, and combination of longer chain hydrocarbons and oils" Steam/methane recombination can be carried out using at least one catalytic reactor, and Snow-helium synthesis can be carried out using at least one catalytic reactor. The reactor may contain various catalysts. As described above with respect to Figure 1, it is the reason why the production rate can be changed. Some of these changes are long-term changes in months or years, while others are short-term changes in hours or minutes or less. Short-term changes are generally relative average -20- 201006919 Gas flow rate is in the range of +/- 20%. In general, the unit and all oil production facilities are shut down once a year for maintenance. The device is preferably adapted to any such variations and fluctuations. A still further aspect of the present invention is a method of reusing a reactor module, the method comprising: removing a module from the apparatus of the present invention, transporting the module to a location remote from the device, and repairing or replacing the presence in the module The catalyst of this or each reactor. If the module is removed because the productivity provided by the module is no longer needed, the module can be refurbished and reused for devices at different locations. ® The present invention also encompasses a process in which an ITM-containing reactor is used for the synthesis gas production, and a catalytic reactor is used for the Fisher-D-Synthesis, at least the Fisher-Serium synthesis reactor contains a catalyst, and the method therein. The replacement of the catalyst involves the removal and replacement of the synthesis reactor and, if desired, the synthesis gas reactor. 'Over time, the reactor may need to be replaced and/or refurbished for a number of different reasons, some of which have a more severe effect on the performance of the reactor. The phrase "reactor needs to be replaced" should not be taken to mean that the reactor must be discontinued. In particular, the replacement of the reactor can be scheduled in advance. For example, each reactor can be scheduled to be replaced after 4 or 5 years of operation, regardless of whether its performance has deteriorated. In this case, the reactor is said to need to be replaced. It removes the module from the device, transports it to a location away from the device, and repairs it. When the module is removed, it can be replaced by substantially the same module if it is desired to maintain device productivity. If the module is removed because the productivity provided by the module is no longer needed, the module can be refurbished and reused for devices at different locations. Renovation may, for example, involve replacing the catalyst, removing the blockage, or removing the body from the upstream fracture within the treatment device. Regardless of whether the catalyst is consumed or not, the catalyst replacement -21- 201006919 can form part of the renovation. If the level of productivity is to be maintained, the reactor is replaced so that the method continues to operate in a non-changing manner. In addition, if there are multiple identical reactors in parallel, only one of them is removed at a time, then the removal of the reactor does not require the suspension of all methods. Renovation facilities can be kept away from installations or oil production facilities. As a result, the GTL device or the oil producing facility does not have to have any catalyst processing equipment. The present invention also provides a method in which a catalytic reactor is used for steam/methane recombination, and a catalytic reactor is used for Fisher-Merco-Synthesis, the counter-reactor contains each catalyst, and the method thereof involves touching each contact The medium is removed and replaced with a recombination reactor or a synthetic reactor. Further in accordance with the present invention there is provided a method for producing an oil producing facility which produces associated gas with oil, wherein the method involves separating the gas from the oil and recombining the vapor/methane with a processing unit incorporating the oil/gas separator. Process gas - a step of synthesizing a synthesis gas, subjecting the synthesis gas to Fisher to form a longer chain hydrocarbon, and then combining the longer chain hydrocarbon with the oil, wherein the vapor/methane recombination system uses a plurality of identical modularizations connected to each other The catalytic recombination reactor is carried out, and the Fisher-Systria synthesis system is carried out using a plurality of identical modular catalytic synthesis reactors connected to each other, the reactor containing each catalyst, and wherein the method involves removing the reactor when the reactor is to be replaced And replacing the recombination reactor or the synthesis reactor. The oil production facility may include a floating production storage and offloading vessel on which the method is practiced. The number of parallel reactors for recombination and Fisher-Synthesis can be at least three. This method may further include removing and replacing the recombination reactor or the synthesis reactor when the catalyst is to be replaced. Additionally, the method can further include moving the removed reactor to a remote processing facility for refurbishment. -22- 201006919 Further, in accordance with the present invention, a method for producing an oil producing facility that produces associated gas with oil is provided. The method comprises separating a gas from an oil, treating the gas with a treatment device combined with an oil/gas separator to produce a synthesis gas, synthesizing the synthesis gas to accept Fisher to form a longer chain hydrocarbon, and then combining the longer chain hydrocarbon with the oil. step. Syngas production is carried out using a plurality of identical modular syngas reactors connected to each other. Each of the syngas reactors includes a plurality of ceramic membranes separating the channels carrying the methane-containing gas stream and the channels carrying the oxygen-containing gas stream, each of which allows the oxygen ions to diffuse through. The Fisher-Symmetric synthesis is carried out using multiple modular catalytic synthesis reactors connected to each other ® with the respective catalyst. The method further includes removing and replacing the synthesizer reactor or the synthesis reactor when the reactor needs to be replaced and/or refurbished. Associated gases typically require additional 'adjustment treatments prior to steam/methane recombination, such as removal of any residual mercury, chloride and sulfur, and if the associated gas contains C2 + hydrocarbons, it is preferred to undergo pre-recombination to These C2+ hydrocarbons are converted to methane. It is advantageous if the process recycles the water produced by the Fisher-Symmetric synthesis to provide a vapor for the reconstitution, since the clean water consumption of the process is minimized. In any case, the Fisher-阙 synthesis produces water that is similar in volume to longer chain hydrocarbons, and the water produced can only be disposed of as waste. Another by-product of the GTL process may be hydrogen because the vapor/methane recombination reaction produces excess hydrogen that is required to exceed the Fisher-Dynamic synthesis reaction. This hydrogen can be separated from other gases after the synthesis gas is produced and/or after the Fisher-Merck synthesis, and can be used as a source of energy for combustion (heat) or to provide mechanical or electrical fuel, such as power to operate the GTL process. . Syngas -23- 201006919 Manufacturing requires heat, which is advantageously provided by combustion of methane or natural gas, preferably using catalytic combustion, although some hydrogen can also be used for this purpose. Preferably, the synthesis gas production (especially by steam/methane recombination treatment) is carried out at a pressure of from 1 to 15 bar abs. The Fisher-阙 synthesis is preferably carried out at higher than 18 bar. The pressure at which the synthesis gas is produced determines the minimum number of compressor stages required, as each compressor stage is practically increased by about 2 times the pressure. Ideally, the synthesis gas is produced at a pressure that minimizes the number of compressor stages by β because the compressor is an expensive part of the equipment. Preferably, the synthetic gas production system is carried out between 2 and 6 bar, so the number of compressor stages is between 2 and 4. However, it is possible to operate a syngas reactor at a pressure above 15 bar using a helium technique, which is similar to the pressure required for Fisher-Dynamic synthesis. The results 'reduced the number of compressor stages required between the ITM syngas reactor and the FT reactor compared to the typical steam/methane recombination reactor and FT reactor required in known small systems, and used The ITM technology can even eliminate the compressor requirements between the syngas reactor and the FT reactor. 在¥ Where the synthesis gas is produced by steam/methane recombination, the recombination reactor contains a recombination reaction channel adjacent to the channel for supplying heat. Preferably, the heat supply channel is a combined catalyst such that the heat system is produced by catalytic combustion. Preferably, the maximum temperature in the heat supply passage does not exceed 8 15 ° C, more preferably does not exceed 800 ° C. Therefore, the maximum temperature in the recombination passage is preferably not more than 800 ° C, and more preferably not more than 780 ° C. This operating temperature is sufficiently low that it is easy to determine conformance to the structural code, particularly the welded structure. The synthesis gas is subjected to a compression of -24,069,069,19 between the synthesis gas production and the Fisher-Synthesis synthesis. It is preferably in the 2 or 3 continuous compressor stages, and the condensed water vapor is cooled and removed during the continuous compressor stage. . The Fisher-阙 synthesis is preferably carried out at a pressure of from 18 to 28 bar (absolute), more preferably from 24 to 27 bar (absolute), and most preferably at a pressure of about 26 bar (absolute). The synthesis gas can also be treated prior to the Fisher-Dry synthesis stage to remove some excess hydrogen, for example using a hydrogen permeable membrane, such that the ratio of hydrogen to CO in the synthesis gas fed to Fisher-Stron synthesis is between 2.05 and 2.50. Good range from 2.1 to 2.4. Fisher-阙 synthesis can be carried out in a number of successive stages, which condense and remove water and longer chain hydrocarbons between the process and the next stage. In this case, it is desirable to use multiple modular synthesis reactors operating in parallel at each stage. In summary, the present invention effectively continuously increases the amount of crude oil provided by the well by adding longer chain hydrocarbons to the crude oil. For example, the amount of oil can be increased by about 5 to 20%. This can also increase the economic life of the well. It also significantly reduces the amount of gaseous hydrocarbons that are burned at the point of production, which is environmentally beneficial and may develop wells that were previously unacceptable. Since only longer chain hydrocarbons are combined, there is no need for additional storage or transportation equipment, and there is no need to seek a separate market for longer chain hydrocarbons. Further in accordance with the present invention there is provided an apparatus for treating natural gas comprising two or more modules connected in parallel; wherein the apparatus is configured to convert the companion gas into a higher density material. As used herein, a "material" can be a solid, a liquid, or a gas. It has many different ways to increase the density of natural gas. It allows the gas to be subjected to physical methods such as cooling or compression to produce liquefied natural gas (LNG) or compressed natural gas (CNG). Alternatively, the density may be increased by chemical methods involving the use of one or more catalytic reactions to treat the product to produce a liquid product in ambient conditions. In this context, "surrounding conditions" means atmospheric pressure and temperatures from 5 ° C to 3 (TC range. An example of a chemical method that increases gas density is the gas-liquid (GTL) method, especially a methane in natural gas. A method of converting to a higher molecular weight hydrocarbon (generally C5+). Other chemical methods that increase the density convert the gas to urea, olefin, methanol, or dimethyl ether. Further an advantage of the present invention is that at least one module is A powerful module. A powerful module is a mode that is subject to transient changes in the conditions of the tolerant method (such as temperature and/or pressure changes accompanying load and output changes that occur when one or more reactions are initiated or turned off in the module). Groups. Transient changes in process conditions may also occur as a result of changes in gas specifications. In addition, changes in the desired product output from the self-funded snow-sleeve module may result in changes in process conditions. Procurement and/or operation of strong 'force modules are It is more expensive than non-powerful modules. Therefore, in the context of this manual, - a module that is not classified as "powerful" is called "economic." Each module can contain two or more series or parallel connections. A reactor or a combination thereof. The reactor comprises one or more ruminal regions connected by one or more headers. The size of the reaction zone is limited by manufacture. The reactor may consist of one or more reaction zones. Where the reactor comprises more than one reaction zone, the zones may be fixed together to form a single large reactor with a single common header, or several reaction zones may be connected via a smaller set of headers. It may be referred to as a reactor. Two or more reactors in series may be provided to perform a two-stage reaction in a single module. These two-stage reaction zones are provided to form two different reactors, or the two-stage zone may be interspersed, For example, it may be staggered. It may preferably be -26-201006919. The second stage reactor is configured differently than the first stage reactor, for example, the first stage reactor can be stronger than the second stage reactor. Providing two or more parallel reactors to increase the overall capacity of the module beyond what can be achieved with a single such reactor. Two or more modules can be a synthesis gas produced with one or more syngas generating reactors The module, and two or more modules, can be a Fisher-阙 module with a Fisher-阙 reactor. All syngas generation modules can be placed in parallel; and all Fisher-阙β modules can be placed in parallel By placing a module containing reactors for performing the same reaction in parallel, it is possible to remove one module without interrupting the activities of the remaining modules. It may have at least 5 syngas generating modules arranged in parallel. Group; and there may be at least 5 Fisher-阙 modules placed in parallel. - Outputs of multiple syngas generation modules may be connected to a common output manifold. Manifolds are provided to aggregate outputs from multiple syngas generation modules The difference in output of these modules can be eliminated. It can also be the case where the number of syngas generation modules is different from the number of Fisher-阙 modules. The syngas generation module can be configured to be regenerated using steam/methane. Syngas. If the percentage of C〇2 in the accompanying gas is high, other recombination methods can occur simultaneously with steam/methane recombination. For example, anhydrous recombination and partial oxidation can occur. The syngas generation module can be configured to produce syngas using an ion transfer membrane. The syngas generation module can further include means for generating vapor using thermal energy output from syngas generation -27-201006919. The syngas generation module can further comprise a reheater coupled to the combustion gas outlet. The reheater is configured to take heat from the exhaust port of the combustion passage. The syngas generation module can further comprise at least one preheater and / or at least one pre-recombiner. Each Fisher-阙 module may comprise: at least two Fisher-阙 reactors connected in series, and a preheater and a phase separator for connecting the output of the first Fisher/阙 reactor to the outside of the module. means. By providing a conduit or the like to feed the output from the first Fisher-Syringe reactor to the phase separator and preheater outside the module, these auxiliary components can be shared by more than one module, and it is not necessary to surround In the module. Since the phase separator and the preheater do not easily have the same life as the reactor, it is advantageous outside the module, so that the module can be removed and replaced at different times when the phase separator and the preheater are replaced. The Fisher-阙 module may further comprise at least one preheater and at least one phase separator. The number of modules can be chosen so that the size of the unit is 100% of the associated gas produced by the treatment oil ® well. In fact, it provides at least one redundant module under normal operating conditions. If excess modules are retained, they provide additional capacity as the gas flow rate increases. However, since the module is not turned on, any catalyst is not degraded by use, and if the excess module is kept open as an active part of the device, the device as a whole can be further lowered. This guides the construction of the preparation and installation of the body and the gas of the hands of the gas with the oil and the oil is taken in the pumping for the storage of the well storage 1 oil description for the connection to support the support for the hair The cost of the type of one according to the allocation: the species contains a package and preparation · 'Setting the tube -28- 201006919 processing unit. This manufacturing conduit can be attached to a subsea or other land well. The unit can be located on a fixed or floating platform. If the well is a subsea well, it may also provide a system configured to secure the treatment unit to the seabed. However, this processing unit can be placed dynamically, so it does not have to be fixed. The unit here can be FPSO » This equipment can further include means for separating oil from associated gases. Separation of oil from associated gases can occur at the well or processing unit. Further in accordance with the present invention, there is provided a method of processing an associated gas source of one or more oil wells, the method comprising providing a modular device comprising two or more parallel modules, at least one of which is a powerful module and At least one module is an economic module; one or more modules are down-regulated when productivity is reduced; at least one or more modules are closed when productivity drops below a reduction limit' 〇 - when productivity drops below the lower limit Closing one or more modules allows the remaining modules to continue to operate within acceptable down-limits, even though the overall productivity of the well is reduced to a level that is too low for a single non-modular device to cope with. For a device containing n syngas generating modules, a module can be turned off when the flow rate of the associated gas body drops below 100 (11-1) / 11% of the total capacity. The lower limit of each module can range from 50% to 60%, so it is practical for the device of η>2 to close a module before the device as a whole reaches its closing limit. If the decline in productivity is only expected to be short-term fluctuations, the module that is turned off when the flow of the associated gas body falls below the lower limit that becomes unusable can be a powerful module. The power module is turned off first in this case because the powerful module -29-201006919 can tolerate faster temperature changes, so the power module can be resumed more quickly when the gas flow rate increases again. If the device is a GTL device, the power module can have a higher thermal inertia than the economic module. If the fluctuations are very short, the power module can still be close to the operating temperature, so it can be resumed very quickly. In comparison, the economic module cools more and is more sensitive to increasing temperature back to production temperature. The method can further include the step of closing a module when the flow rate of the associated gas drops below a predetermined lower limit for more than a predetermined time. For example, in a system with β 5 modules, if the flow rate of the associated gas drops below 80%

For 6 months, it is an indicator of long-term decline in oil well productivity, as shown in Area C of Figure 2. In this case, it can turn off one of the modules and can be removed. in this way. It helps the remaining modules to process deeper associated gas extractions only through down-regulation. Continuation • In the above example, the remaining 4 modules can cope with the fluctuation of the associated gas flow to 40% of the initial productivity (80% of the 50%), so the dependence on the powerful module is reduced. Closing and removing modules also increases the overall utilization of the modules, as closed modules can be removed and redeployed to devices in different wells. 模组 Modules that are closed in this case can be economical modules. In order for the device to retain the maximum flexibility of the process gas flow fluctuations, it is important that at least one of the power modules remain within the device. Therefore, the module that is first turned off should be an economic module. This module can then be removed from the device for renovation or service or redeployment elsewhere. The modular device can be configured to convert the associated gas to liquid hydrocarbons wherein the liquid hydrocarbons are combined with oil from the well. Combining synthetic crude oil or liquid hydrocarbons with -30- 201006919 The solution to the associated gas problem from crude oil in the well is because the treatment oil itself does not require additional transportation infrastructure. The modular device can be configured to perform the steps of: separating the associated gas and oil; treating the gas in the first catalytic reactor to produce the syngas; and synthesizing the syngas from the synthetic snow to form a liquid under ambient conditions. Long chain hydrocarbons. Additionally, the apparatus can be configured to provide at least an economic syngas generation module that uses methanol as a combustion fuel during short term productivity reductions. If the flow of associated gas is reduced to a very low level in a short period of time, such as a disruption in well activity, the accompanying gas flow may suddenly drop to almost zero. In these cases, in order to maintain the operating temperature of the syngas reactor at the time of resumption of work, it is appropriate to close all modules and provide an economic module with methanol as fuel. Depending on the availability of methanol and the time of deactivation, it is provided.  It is appropriate to use methanol as a powerful module and economic module for fuel, or to naturally cool the powerful module to ambient temperature. In addition to or instead of using methanol or other liquid fuels, in order to maintain the module at the operating temperature, it can use hot exhaust gases from this method anywhere in the unit. In particular, it can use exhaust gas from a diesel combustion process. In addition, electric heating can be provided within the module, and it can be used in addition to or in lieu of the alternative gas supply listed above. Further in accordance with the present invention, a control system is provided to operate the above apparatus in accordance with the above method. This control system can take advantage of the sufficient maneuverability of the device. In order for the composition of the output to conform to or complement the composition of the oil from the well, the control system may further comprise means for monitoring the composition of the synthetic crude oil leaving the Fisher-Tropsch reactor -31-201006919, and for modification The means of the conditions in the Fisher-阙 reactor. The temperature in the Fisher-阙 reactor and the composition of the syngas have a significant effect on the proportion of different liquid hydrocarbons produced by the reactor. Thus, by varying the temperature of the Fisher-Tropsch reactor, the composition of the resulting synthetic crude oil can be modified to conform to the composition of the oil output from the well. In some cases, it may be preferred to select a composition of synthetic crude oil such that it complements rather than conforms to the composition of the oil from the well. The term "oil production facility" means a facility in which oil flows from an oil well to one or more wells ® and is at least initially treated prior to storage or pipeline transfer. For example, it may refer to a fixed platform or a floating production storage and offloading (FPSO) vessel. In general, this facility is connected between 1 and 20 separate wells in a single field. It can also refer to small facilities such as oil well test vessels. The terms "integration" and "combination" mean that the GTL device has been separated from the oil.  The gas is obtained afterwards without requiring a large amount of chemical treatment. Thus the GTL device of the present invention can accept both treated and untreated gases. The term "identical" means that the reactor system is configured to have substantially the same ® performance and a compatible connection to the flow conduit (for reactants or coolant) so that one reactor can be easily installed in place of the other. Once installed, the same reactor has substantially the same output and chemical properties as the substituted reactor. It should be understood that the chemical properties of this reactor may be different, for example due to aging of the catalyst. The shape and size of the modular reactors are not necessarily the same, although it may be economical to manufacture the same reactor, which may be preferred. As used in the context of the present invention, the term "small" includes a reactor which provides a large surface area for the catalyst and heat exchange in a small volume. In particular -32- 201006919 Small reactors are manufactured and configured for use in oil production facilities. In order to be used in oil production facilities, the reactor is sized to be mounted on a fixed offshore oil flat or FPSO vessel. To facilitate installation, maintenance, and removal of the reactor, the mold is desirably sized such that it can be processed by conventional cargo handling equipment. For example, a small reactor should be sized to fit into an ISO container and weigh no more than ton. Small reactors generally have the ability to handle about 60,000 cubic meters per day of associated gas. The term "synthesis gas reactor" or "syngas source" as used in this specification refers to a reactor for producing a synthesis gas when a suitable hydrocarbon-containing feed gas is supplied. [Embodiment] The apparatus and method of the present invention can be applied to a well producing an accompanying gas with oil, wherein the gas oil is preferably between about 35 and 350 cubic meters per cubic meter - refer to Fig. 2, which is shown in a schematic manner Indicates that productivity P has moved over time. As indicated by the solid line, the oil well starts to produce oil with productivity P, which generally increases (A) and then reaches the plateau (B). Productivity P then maintains its true V for several years, but then begins to decline (C), and this decline lasts for several years. When the present invention is used, the productivity change is indicated by a broken line (D). Productivity is slightly higher in all operations of the well because it combines the conversion of raw gases into longer chain hydrocarbons, thus increasing the amount of oil in the well. The higher productivity of the outer well indicates that the economic operation of the well can last longer. As described above with respect to Fig. 1, the associated gas production rate G derived from the oil well is changed in a manner similar to the variation of the productivity P of the oil. Referring now to Figures 3 and 4, these figures show an alternative procedure for implementing the process unit 10 of the counter-oil 〇 〇 上 以 以 - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - In all of the following descriptions, substantially identical components in the apparatus illustrated in Figure 3S use the same reference numerals. Figure 3 shows a flow diagram of a processing apparatus in which syngas is recombined by steam/methane. Figure 4 shows a flow diagram of a process for producing syngas using an ion transport membrane. In the processing apparatus shown in Figs. 3 and 4, the fluid produced by the well (indicated by "feed") is fed to the separator 11, wherein the oil 12 is separated from the associated natural gas 13. The oil 12 is stored in the oil reservoir 14 β . The associated gas 13 is then adjusted to remove impurities, which are first washed by water spray (or by cooling and coalescing the aerogel of the droplets), then the mercury is removed 16 and then passed through the heat exchanger 17 And then let it accept sulfur removal 18. The natural gas stream is thus produced, typically about 90% methane and less than 100% other paraffins. - The treated natural gas is then combined with high temperature steam and heated by a second heat exchange 20 to a temperature of about 400 °C. It is then subjected to pre-recombination 22 (which, for example, using a nickel catalyst); thus any C2 + hydrocarbons (ethane, propane, brothel, etc.) are converted to a courtyard and carbon monoxide, and if the natural gas 13 contains a slightly higher proportion The alkane does not require pre-recombination 22. This flow system selects the previous recombination treatment 22 to provide a suitable vapor: methane molar ratio. For example, in the example shown in Figure 4, the steam to methane ratio can be 〇: 1 to 1. 5:1 range. Or in the example shown in Figure 3, the steam to methane ratio is 1. 4 to 1 and 1. 6 to 1, more preferably 1. Between 5 and 1. The gas mixture (which consists essentially of methane and vapor) is then passed through a plurality of fluidized reactors 24, 14 through the same modular synthesis gas. In the process shown in Figure 3, each reactor 24 is defined to contain a recombination catalyst (such as an aluminoxy support). The channel for the vapor/methane recombination reaction of platinum/ruthenium catalyst. The additional channels provide heat from catalytic combustion and contain a combustion catalyst (e.g., platinum or palladium catalyst on an aluminoxy support). The gas supplied to the combustion passage may contain air and methane, and the methane supply is obtained from natural gas at the outlet of the desulfurization method 18. The hot exhaust gas using the combustion passage (indicated by the dashed line 26) is then heated by the gases of the heat exchangers 20 and 17. Upon passage through the recombination channel, it heats the gas mixture to a temperature of about 75 (the highest temperature of TC, and reacts methane with steam to form carbon monoxide and hydrogen, which is endothermic. The resulting mixture of carbon monoxide and hydrogen is referred to as synthesis gas or syngas. In this case, the hydrogen to CO ratio is about 3: 1. The gas pressure in the recombination channel is 2. 5 bar (absolute) = 〇. 25 MPa 〇 In the method illustrated in Figure 4, each reactor 124 comprises one or more sheets - ceramic sheets (oxygen ions can diffuse through), as described in, for example, U.S. Patent No. 7,279,027, the disclosure of which is incorporated herein. For reference, it can be packaged in a pressure vessel and can be combined with a vapor/methane recombination catalyst as described in U.S. Patent No. 7,179,323. The reactor defines separate channels for reactants (e.g., vapor/methane mixture) and oxygen-containing gases (e.g., air) that are separated by a ceramic membrane that diffuses oxygen ions into the methane-containing stream. It preheats the gas supplied to the two passages, for example, by passing through a reactor 123 along a flow passage adjacent to a passage in which combustion occurs (or exchanging heat in the heat exchanger with hot exhaust gas from the combustion method). Preheat reactor 123 is equivalent to heat exchanger 20, but is disposed after front reformer 22. If the reaction occurring in reactor 124 is sufficiently exothermic (depending on the proportion of vapor with methane feed and the rate at which oxygen ions are diffused into the reaction environment), the outflow gas may be sufficiently hot At least a portion of this is provided by heat exchanger 30, as shown. Preheating the gas contributes to the rate of partial oxidation reactions occurring in the reaction channels. The results provide overall simplification using ITMs compared to known vapor/methane recombination reactors because no separate thermal methods are required within the ITM reactor 124. Exhaust gas from the combustion process in reactor 123 can then pass through exchanger 20 (as indicated by the dashed line 1 26). At the outlet of the syngas 24, 124, the resulting synthesis gas is quenched by a heat exchanger 30 to provide a vapor (as indicated by line 31) supplied to the inlet of the heat exchanger 20. The synthesis gas can then be cooled (not shown) to undergo one or more successive compression stages 32 (two stages 32 are shown in Figure 4, and three stages are shown in Figure 3), and 33 condensed water vapor is removed after each compression stage 32. • If necessary, ensure that the synthesis gas is the pressure required for subsequent Fisher-Dynamic synthesis.  , which can be, for example, 26 bar (absolute) = 2. 6 MPa. The synthesis gas is passed through a carbonyl nickel trap 36 and then to one or more Fischer-Tropsch synthesis reactors 40 flowing in parallel. In the provision of multiple Fisher-阙 synthesis reactors 40, the Vendor 40 is modular and identical. Each reactor 40 defines a channel for the Fisher/Relief reaction containing a suitable contact (e.g., cobalt on an aluminoxy support) and a heat exchange fluid to remove the heat generated by the synthesis reaction. The heat exchange flow system is circulated (shown graphically) by the temperature control system 44, and the speed of the heat exchange fluid is such that the temperature it increases through the counter reactor 40 is maintained within a desired limit, such as no more than 10 K. The fluid mixture from the synthesis reactor 40 is cooled by a heat exchanger and separated into water by a separator 48, a liquid hydrocarbon C5+, and a residual tail to heat up and heat up.  Or after the snow 9 media exchange flow 46 gas -36- 201006919. The coolant for heat exchanger 46 can be a fluid, such as water, and can be at a temperature of, for example, about 20 or 30 ° C, or more preferably a slightly elevated temperature, for example, to between 80 ° C. This higher temperature coolant substantially prevents deuteration of the inner surface of the heat exchanger. Water from separator 48 is recycled to quench heat exchanger 3 0 ' as indicated by dashed line 31, although it may be first treated to remove any mass. The liquid hydrocarbon C5+ from the separator 48 is combined with the oil 1 2 in the storage tank 14 to increase the volume of the oil. Mixing of the liquid hydrocarbon c5+ with the crude oil 12 can occur upstream of the storage tank 14. Synthetic reactor 40 with output temperature control system 44 ❹ output heat exchanger 46 and separator 48 may be referred to together as composite assembly 50. The off-gas feed from separator 48 is passed through this composite 50 (shown graphically) and the gas from the second synthesis assembly 50 is fed back to the inlet of heat exchanger 20. * In the apparatus 10 of Fig. 3, the gas produced by the steam reforming reactor 24 has a hydrogen:CO ratio of about 3:1, and the Fisher-阙 reaction requires a ratio of 2:1 in terms of chemical amount. There is therefore excess hydrogen in this process. In this scheme, some of the high pressure synthesis gas from the outlet of the thiol nickel 36 is separated by a membrane unit 38 to separate some of the hydrogen, preferably through a membrane unit 38 flow system such that it is in the Fisher-Syringe reactor 40. The hydrogen at the inlet: c〇 ratio is nearly 2:1, for example 2_4 to 2. Between 1:1. The tail gas from the second synthesis assembly 5 also contains some hydrogen, and this gas stream is also passed through the membrane unit 52 to be removed so that the recycle gas stream fed back to the inlet of the heat exchanger 20 is mainly composed of short chain hydrocarbons, carbon monoxide, carbon dioxide, Composition with water vapor. In the apparatus 10 of Fig. 4, depending on the composition of the body mixture supplied to the ITM reactor 124, the synthesis gas cycle 60 46 produced by the ITM reactor 124 is replaced by the total dispersion of the group tails ( j院气体-37- 201006919 can have a hydrogen:CO ratio of up to about 3:1 (syngas ratio), which is the ideal stoichiometry required for non-Fisher/阙 reaction. If there is excess hydrogen, then upstream of the FT reactor Some of the synthesis gas may diverge through the membrane unit 38 to separate some of the hydrogen, causing the syngas ratio to fall closer to 2: 1. The tail gas from the second synthesis assembly 50 may also contain some hydrogen, and this gas stream also passes through the membrane unit. 52 to remove this hydrogen such that the recycle gas stream fed back to the inlet of the heat exchanger 20 consists essentially of short paraffins, carbon monoxide, carbon dioxide, and water vapor. ❹ The overall result is that it converts the associated gas 13 into a liquid state. The longer chain hydrocarbon C5+ is then combined with the oil in storage tank 14. The by-product water from synthesis assembly 50 is fed back, as indicated by dashed line 31, to provide the vapor of the process. Membrane unit 38 and membrane unit 52 are withdrawn. Hydrogen As a source of fuel may be, for example, provide for the operation of the compressor 32 • use of power.  As explained with respect to Figure 1, the flow rate G of the associated gas 13 changes as the life of the well passes, and in addition (as discussed previously) there are also short-term variations such that the apparatus 10 must be able to handle a wide range of different gas flows. Some of the processing units within the processing unit 10 operate equally well over a wide range of different gas flow rates. However, reactor units (especially syngas reactors 24, 124 and synthesis reactor 40) have particular problems, the performance of which varies significantly with gas flow rate. Thus each reactor 24 and each reactor 40 has a shut-off valve 55 at all of its inlets and outlets (only two are shown for each reactor) so that individual reactors 24, 124 and 40 can be discontinued without affecting the remaining processing unit 1 0 operation. For the steam reforming reactor 24' on the hot side of the process (>500 °C) (ie -38-201006919 thermal process outlet (with hot combustion outlet)), the shut-off valve is optional or each reactor 24 can have a dedicated step The cold heat exchanger, like the hot junction 30, can then be placed on the outlet side of the quench heat exchanger. Also, on the hot combustion side, each reactor 24 may have a heat shut-off valve. An alternative is to provide the reactor 24 with a dedicated recuperator similar to the reheater 20, which may be located at about 200-500 ° C on the exit side of the reheater. In this manner, individual reactors 24, 124 and 40 can suspend operation for the remainder of the plant. © If the flow rate G of the associated gas is increased during operation, the reactors 24, 124 and 40 already in use can be easily reused. It should also be understood that during the full operation of the unit, there are some reactors 24, 124: not used. If one of the other reactors 24, 124 or 40 is malfunctioning, this provides a certain amount of excess. Thus the malfunctioning reactor 24 or 40 can shut down and use other reactors 24, 124 or 40. It is a quick way to remove and replace the reactor. In practice, the shut-off valve 55 can be used in pairs, at least one isolating square valve and one isolating the reactor side valve, and the pair of valves is flushed by inert gas to remove atmospheric oxygen before the reactor is started. The length pipeline comes. In order to effectively isolate the reactor, a blank plate may be provided between the pair of valves. When necessary to close one of the synthesis reactors 40, the shut-off valves 5 5 on the reactor side are closed. At the same time, a self-closing gas supply (not shown) is used as a pressure (in this example, 26 bar (absolute)) inert gas flushing reaction to remove any residual synthesis gas. The connection to the shutdown gas is then also turned off to shut down the reactor 40 at the operating pressure. This ensures the term. The converter is not used to replace the 40, such as '124 ratio shift test and charge separation 〇 40 two with the operator 40 supply. -39- 201006919 The media does not degenerate. Thus shutdown or inert gas is a gas that does not involve a catalytic reaction and substantially prevents further catalytic activity in the reactor. For example, this inertia is pure methane, desulfurized natural gas or nitrogen. Reactors 24, 124 and 40 can be insulated such that they do not cool rapidly after shutting down in this manner. In fact, when processing a short-term drop in gas flow, it may be desirable to provide a source of heat to reactor 24 or 40 so that once reactors 24, 124 are reconnected, they can return to full load operation more quickly. It should also be understood that this step removes and replaces unused individual anti-, eg, if the reactor requires refurbishment (eg, replacement of spent catalyst). The reactor can be transported to a remote location (for example, replacing the catalyst). There is no need to provide catalytic treatment equipment at the oil production facility. The treatment unit 10 is used in an oil production facility and is therefore sized to install a fixed oil platform or an FPSO vessel, or any facility available. In particular, each of the processing units within the apparatus 10 should be sized to handle the shipping equipment so that the processing unit can be installed or maintained. In particular, each of the counters 24, 124 and 40 should be no more than about 25 tons and be small enough to fit within the size of the name V container. For example, each of the reactors 24, 124 and 40 can have a capacity of 10 tons, a total length of about 8 meters and an associated gas 13 suitable for processing about 60,000 cubic meters / Mscf / day. The reactors 24, 124 and the detailed configuration are not in the form of the present invention, but it should be understood that each reactor is a small reactor, i.e., provides a large volume for heat exchange (also used in catalysts for catalysts). Surface area. In the ITM syngas reactor 124, the channel is typically zero. Between 3 5 mm high (minimum lateral dimension), and vapor/methane recombination, due to gas available, removed at 124, 40 or 40. Because the E ISO of the solid-state conditioning device is about 1 day (the required combustion channel and the recombination channel in the range of 2-40 must be supplied to the instrument-40-201006919 24, the height is usually 1 to 5 mm high (minimum lateral dimension). In the synthesis reactor 40, the coolant passage is generally between 1 and 5 mm high, and the Fisher-阙 reaction passage may be slightly higher, typically between 4 and 12 mm high. In the channel, the catalyst may be provided as a coating on the wall of the channel, or as a bed of catalyst particles, or as a coating on a metal substrate in the insertion channel. The catalyst insert may subdivide the channel into a plurality of parallel secondary channels. For example, a corrugated foil. The reactors 24, 124, 40 in Figures 3 and 4 are shown as separate reactors connected in parallel. However, it should be understood that this figure is only for illustration. In practice, the manufacturing steps are applied to the reactor zone. Effective reactor system. Each reactor 24, 124, 40 may comprise one or more reactor zones. In order to carry out the reaction in two stages, the zones of each of the reactors 24, 124, 40 may follow the second reaction of the same type. Displaced,  Moreover, each zone has a header tank to cause fluid flow to move from one reactor to the next. Adjacent zones can be held together, whether or not they form part of the same reactor. If the adjacent zones are all identical reactors, a single beta-common header can be connected to all reactors. A module can be defined as part of a device that can be isolated from the rest of the plant without compromising the operating force of the device. Modules can be combined or not. The means required to isolate them, such as shutting off the valve. In the context of the apparatus shown in Figures 3 and 4, the module may be reheated with or without a shut-off valve 55 and/or a similar heat exchanger 30 and/or a reheater 20 A single reactor 24, 124, 40. Or the module can be defined as a part of the device that can be independently removed from the device after isolation. If the module is to be removed independently, -41-201006919, in order to isolate the rest of the plant from the module to facilitate removal of the module from the device, it must provide a shut-off valve similar to valve 55 at least outside the module. Depending on the components of the module, one or more valves external to the module are not provided to provide one or more additional valves as part of the module. In a further alternative, one or more of the modules can be removed once the module has been isolated from the rest of the plant. To facilitate this, a valve can be provided between the components of the module. This configuration is advantageous in situations where the module contains several reactors and other components, such as quench heat exchangers and/or preheaters and/or pre-recombination managers. If one of the reactors in the module fails, all modules can be isolated to make the rest of the plant sustainable. However, in addition to removing all modules, the error reactor can be isolated from the rest of the module and can be removed separately. In this case, the error reactor itself is also effectively 'as a module' because it can be isolated and removed. - Figure 5 shows several different module configurations. The various configurations shown in Figure 5 only show the processing flow through the module. In the fully illustrated configuration, the processing flow takes place from left to right in the diagram. Further numeral 24 has been used to indicate an example of a reactor for syngas generation. However, it is obvious that the fully described module configuration is equally applicable to the situation when syngas generation occurs in a reactor 1 24 operating ITMs. The simplest configuration for forming a module for processing a portion of natural gas 500A is shown in Figure 5A. In this configuration, each module 501, 502 consists of only a single reactor 24,40. Once the associated gas has been pretreated, it is introduced into a first module 501, which is a syngas generation reactor 24. The synthesis gas leaves the first module 501 and is prepared in the other parts of the device - Fisher - Co. -42 - 201006919. The syngas is then introduced into a module 502, which is a reactor 40 where Fisher-阙 synthesis is performed to produce synthetic crude oil. This configuration is equivalent to the device detailed in Figures 3 and 4. Figure 5B shows a device 500B comprising two modules 503, 504, each comprising two reactors operating in series. It occurs in the second stage of syngas generation in the module 503, and a two-stage Fisher-阙 synthesis occurs in the module 504. In each case, the module may include one of the processing stages or other means of fluid flow, such as after the first stage of Fisher's synthesis, subjecting the output to cooling, ❹ phase separation, and preheating 76. These steps are collectively referred to as inter-stage processing 70. Figure 5C shows a syngas generation module 505 in which a waste heat boiler or steam generator 30 is inserted into the module. . In addition to the reactors 24, 40, the module can include a separator 24, 40.  Off the valve. By providing a valve within the module, the reactors 24, 40 can be isolated from any other components within the module. In this manner, the reactors 24, 40 can be removed from the module. Alternatively, only valves may be provided to isolate the module from the rest of the plant. The valve is not illustrated in any of the examples shown in Figure 5, and it should be understood that in each case the valve may be provided in the module in addition to or instead of a valve placed outside the module to isolate all modules. Figure 5D shows a GTL module 506 comprising two syngas generation reactors 24, a waste heat boiler or steam generator 30, a compressor 32, and two Fisher-Heap reactors 40. It performs phase separation and preheating between the two stages of Fisher-Synthesis. However, because the components required for these activities are not included in the module 506, the output of the first Fisher-Syringe reactor is distributed out of the module that accepts the phase separation, and then the second phase of the Fisher-Synthesis is introduced. Pre-heating of module 506 -43- 201006919 provides the results of syngas generation and Fisher-阙 synthesis in a single module 506, which may be referred to as a train. Figure 5E shows a syngas generation module 507, similar to that illustrated in Figure 5C, except that module 507 contains four syngas generators that provide two-stage syngas generation. There are two parallel reactors in each stage. The outputs of the two first stage reactors are combined in manifold 99 before being separated and fed to the two second stage reactors. The output from the two second stage syngas producing reactors is then introduced into a heat exchanger 30 or a waste heat boiler where steam from the synthesis gas is used to generate steam. Providing manifold 99 eliminates any difference in the performance of the two first stage reactors such that one of the second stage reactors is not undesirably lower than the optimum performance of one of the first stage reactors. - Figure 5F shows a syngas generation module 508, similar to that illustrated in Figure 5E, except that the front recombiner 22 is inserted into the module 508. Figure 5G shows the Fisher-阙 module 509, which includes three parallel lines of a two-stage Fisher-阙 ® synthesis reactor 40. The syngas is first preheated in the preheater 76. After the first stage of Fisher-Synthesis, it combines the outputs from the three first stage reactors and undergoes cooling, phase separation and preheating in interstage process 70. The output from the preheater is equally divided between the three second Fisher-Stron reactors 40. Figure 5H shows a module 510 comprising three parallel Fisher-阙 modules. In order to provide a two-stage Fisher-阙 synthesis, the module 5 10 is combined in series with other similar modules. Alternatively, two modules 510 of -44-201006919 may be provided in parallel for the first stage of Fisher's 阙 synthesis, and then a single module may be provided in parallel for the second stage of Fisher-阙 synthesis. The single module may contain only five parallel reactors 40 compared to six of the two parallel modules 510. In order to manufacture a GTL device, it combines several modules as shown in FIG. In general, the apparatus consists of a plurality of modules 501, 503, 507, 508 comprising syngas reactors 24, 124, and a plurality of modules 502, 504, 509, 510 comprising Fisher-Synthesis Reactor 40. composition. An example of the configuration of a GTL device is shown in Figure 6A. All of the syngas generation modules 5 08 are connected in parallel so that either of them can be turned off, and then removed as appropriate without the need to shut down the remaining modules. Similarly, all Fisher-阙 modules 509 are connected in parallel. Alternatively, the mounting may consist of a plurality of modules 506 connected in parallel, as shown in Figure 6b. • A further example of a GTL device is shown in Figure 6C. This example consists of five two-stage syngas generation modules 5 03 and five two-stage Fisher-阙 synthesis modules 504 » In a very large unit as shown in Figure 6D, it can be introduced The auxiliary components of the process gas prior to the first module 505 containing one or more syngas reactors are modularized. In particular, it can combine the cleaning 15 , the mercury removal 16 , the heat exchanger 17 , and the desulfurization unit 18 into the auxiliary module 600 . The feed gas system is introduced into the unit via a common manifold 601. In the illustrated example, 15 modules 505 are connected in parallel. The auxiliary module 600 can service 5 modules 5 05 containing a syngas generating reactor. Therefore, three auxiliary modules 600 are provided for servicing the 15 modules 505. As the gas well production decreases, the modules 505, 504 are closed and removed, and the auxiliary module 600 is also the same. Parallel provision of more than one auxiliary module 600 as shown in -45-201006919 reduces the extent to which the auxiliary component lower limit adjustment device can be down-regulated as a whole. When considering the overall capacity of the device, a smaller module (whether or not this capacity is obtained from multiple reactors or reactors) provides a small increase. However, devices containing a large number of modules add a large amount of complexity in connecting lines and valves. This adds complexity and increases costs. The size of the modules in the device and the number of modules are therefore a compromise between these factors. In addition, the size of the module is limited by the above requirements for loading it into a standard ISO container.模组 The modular approach to treating associated gases offers a number of advantages over non-modular methods. Previously, the present application has foreseen a modular system comprising two or more substantially identical modules for each reaction (e.g., syngas production and fee, snow-synthesis synthesis). However, in order to create a more flexible and cost-effective system, modules configured to operate in parallel and perform the same reaction can have different properties. .  The power module is a module that includes at least one powerful reactor. Compared to economic modules, a strong reactor is a reactor with improved tolerance for transient changes in process conditions. The strength of the reactor, i.e. its ability to tolerate this transient ® change, can be modified in a number of different ways as described below. In each of the reactors 24, 40 provided in the modules 501 to 510, they may have a plate and fin structure. The plate and fin structure includes a stack of plates 702 interspersed with the forming plates 704, 709. The combination of forming plates 704, 709 and plate 702 defines a flow passage. Alternative groups of flow channels within the stack have different purposes. For example, as illustrated in Fig. 7A, in the syngas generation reactor 24, the first flow passage 76 is configured to contain a carrier catalyst foil, and vapor methane recombination occurs in these passages. Adjacent or second flow channels 708 are configured with -46-. 201006919 A foil containing a combustion catalyst. Since both sets of channels 76, 078 are configured to contain a carrier foil, both sets are defined by a plate 704 having a rectangular tooth profile. The toothed plate 7 04 is shaped to define a plurality of fins 750 extending from the plane of the vertical plate 702. Although the toothed plates 704 defining the channels 706, 708 can be the same as shown in Figure 7A, they can be configured to define channels 706, 708 of different sizes. Conversely, in the Fisher-阙 reactor 40, the first flow channel 706 is configured to contain a carrier-containing foil, but the second flow channel 708 is configured to contain fluid to control the flow from the Fisher-Symmetric channel 706. heat. The plate 709 defining the second flow turbulence channel may have a serrated shape. This configuration is illustrated schematically in Figure 7B. In order to change the strength of the reactor, it can vary the thickness, separation and height of the fins 705. The fin separation 710 is the distance between adjacent fins 7 05 ' extending from the vertical plate 702. a plate with a small wing (eg 2 mm) and a wing structure.  The reactor is more powerful than a reactor with a larger fin (eg 20 mm). The fin height 712 is the distance that the fin extends in the direction of the plane of the vertical plate 702. It is also effectively the distance separating the plates 702. The height of the fins can be in the range of 2 mm to 20 m ® m, and the smaller the height, the stronger the reactor. In order to influence the strength of the reactor, the thickness of the plates 702, 74 can also be modified. In particular, the thickness of the forming plates 704, 709 can be 0. Within the range of 3 mm to 1 mm. The plate 702 can be in the range of 1 mm to 3 mm. Reducing the fin separation and height and lowering the height of the plate 702 increases the heat exchange area per unit volume of the reactor, resulting in better heat transfer, which preferably dissipates instantaneous heat, thereby avoiding constrained structures and causing reactor damage or shortening A large thermal gradient of reactor life. In addition, the reduction of fin separation and height is also -47-201006919, resulting in an increase in the amount of metal in the reactor and an increase in mechanical strength, which results in a heavier and more expensive reactor. The powerful reactor can be fabricated using one or more of the above variations of the plate and fin configuration. As is apparent from the above, the strength is not always synonymous with mechanical strength, because if the thickness of the plate 702 is reduced, the reactor has a lower mechanical strength, but the reactor is more powerful because the thinner plate 702 can increase the flow. The heat transfer between the channels thus reduces the temperature difference within the reactor, thereby reducing the stress on the reactor. The strength of the reactor can also be increased by β by varying the material from which the plates 702, 704 are made. For example, in a reactor configured to perform Fisher-Dynamic synthesis, plates 702, 704 can be fabricated from soldered aluminum. However, in a powerful Fisher-Rich reactor, the plates 702, 704 can be made of stainless steel or titanium. In addition, the manufacturing methods used in economical and powerful reactors can be different. Reactors with plate and fin configurations can be fabricated by welding or diffusion welding. One .  In general, diffusion welding requires a higher amount of metal than the weld, which may be appropriate for a particular type of strong reactor. Alternatively, a strong reactor can be fabricated from metal blocks using wire corrosion techniques rather than by the above techniques. In addition to or in lieu of changes in the materials, welds and plates and fin configurations and materials used in the reactor, catalyst changes can also alter the strength of the reactor. The catalyst can be supported on the ceramic coating on the convoluted or wavy foil introduced into the channel 76. In a strong reactor, the catalyst can be less reactive and increase the length of the treatment, thus resulting in a reduction in thickening, i.e., a reduction in the degree of processing per unit length of the channel. The catalyst can be less active by varying the size of the crystal deposited on or in the ceramic support, or by depositing less catalyst per unit length. In addition, in order to prevent the fluid from approaching the active catalytic material, it provides an inert coating of at least a portion of the catalyst. In order to provide a robust reactor, further changes in the configuration of the reactor can be combined with changes in the plate and fin configuration and/or changes in the catalyst. For example, it can change the number and size of headers. The economic module is one in which all or all of the reactors are economic reactors. The powerful module is a module that contains at least one powerful reactor and is more economical. Usually if the module contains more than one reactor, all reactors in parallel configuration should be equally strong. For example, the two reactors in module 503 can be identical. However, when the two-stage synthesis gas generation is completed, the system conditions can be optimized differently in the two reactors, so that the first-stage reactor can be stronger than the second-stage reactor. Conversely, the two phases of the Fisher-Synthesis are usually operated under substantially the same strip, so if one of the two-stage two-stage Fisher-阙 reactors in the module is a strong reactor, then Both are strong. In order to control the device handling the associated gas, it requires a control system. The equipment for dealing with associated gases faces unique challenges. In most cases, except for devices that process associated gases, they can control device inputs. Conversely, the flow of associated gases varies greatly and is uncontrollable. There are different types of changes in the flow of associated gases and they require different responses. First, as illustrated in Figure 2, the flow rate of the associated gas produced by the well decreases with the life of the field. In order to take advantage of the modular device, the average flow rate of the associated gas produced must be monitored by the control system. The measured flow rate is then subjected to statistical analysis, so that the data is smoothed to avoid improper short-term fluctuations, paying attention to the standard deviation of the average 値. When the average daily flow rate of the gas (-49-201006919 flow rate ratio at full load) does not exceed 100 (nl)/n% (where η is the number of syngas generation modules) for more than 6 months or other predetermined initiation time The control system indicates that one of the modules should be turned off. In this case, it is usually chosen to shut down the economy module to ensure that the device still includes at least one power module. Once the module is turned off, it can be left to provide the redundant module to the device when the remaining modules are functioning abnormally. Or once the module has been turned off, it can be removed from the device for repair and/or redeployment as part of a different device. Depending on the size of the unit and the rate at which the productivity of the well declines, the time between starts can range from 3 to 18 months. For example, if a large device is deployed, the percentage of productivity required to make the module redundant is quite small. In addition, if the productivity of the well decreases rapidly, the initiation time can be only 3 to 6 months. For example, in the device shown in Fig. 6, when the flow rate of the associated gas does not exceed 67% of the full load for more than 6 months, it closes one of the modules 506. Once .  If one of the modules 506 is turned off, only two modules 506 remain, so that the "full load" of the device with two modules is 67% of the original volume. When the gas flow rate drops to 50% of the full load of the two modular devices for more than 6 months, it closes one of the 2 ® remaining modules. In the case where each module contains only a syngas generating reactor or a Fisher-only synthesizing reactor, it removes one module of each type (i.e., a total of 2 modules) from the device. For example, in the apparatus shown in Fig. 6C, one of the modules 505 and one of the modules 504 can be turned off when the average flow rate per day of the gas exceeds 80% for more than 6 months. Secondly, the flow rate of the associated gas is subject to small fluctuations. Fluctuations are random variations in the flow of the associated gas, which represent a deviation of -50-201006919 of at most +/-15% of the average gas flow rate. These fluctuations occur too shortly to allow the module to shut down and respond. Therefore, in order to handle the fluctuations, the control system only raises or lowers the module. When the gas flow drops below the lower limit of the device, it must close the module. The control system selects a powerful module that can be turned off. If the expected gas flow drops more than short-term, the power module can be filled with inert gas and can rely on the thermal inertia of the powerful module to keep the module close to the operating temperature for a longer period of time than the economic module. . It can be applied to various stages of the process, for example in a device as in Figure 3, if the gas flow drops below the down-regulation limit and is expected to fall to short-term, © a strong SMR reactor 24 and a strong FT reactor 40 should be closed. Or it may supply only one method stage, such as syngas generation. In this case, all of the Fisher-阙 reactor 40 can be equally strong. Because the output of a device that processes associated gas from a single well is complexly associated with the production of the well, the control system is configured to respond to the loss of the well. It can be .  Can happen unexpectedly. In this case, the flow of the associated gas drops to zero over a relatively short period of time. In this case, the control system is configured to supervise the control to shut down all modules. Depending on the availability of methanol and the expected loss of gas flow, the control system transfers at least the economic SMR module to use methanol as a fuel. In addition to variations in gas flow into the device, transient conditions may occur in one portion of the device that produce short-term changes in process conditions in other portions of the device. For example, if the method is configured to feed the output of the module back to other modules upstream of the method, a feedback loop can also be generated that can also cause a change in method conditions, which produces a transient change in the overall condition of the method. The carbon content of the exhaust from the Fisher-阙 module is fed back to one or more of the -51-. 201006919 When the front recombiner upstream of the gas generation module is generated, an example of this occurs in a GTL device that includes a syngas generation module and a Fisher-阙 module. When the syngas generation module is initially activated, it generally does not have any exhaust gas from the Fisher-阙 module that can be introduced. Once the exhaust gas becomes available, it is introduced into the pre-recombiner and the feedback loop is closed. Closing this loop causes a brief change in the process conditions in the syngas producing reactor. It is therefore advantageous if the power module is activated first and the feedback circuit is completed. Once the system has been stabilized, the economic module can be brought online. The beta control system also monitors the composition of the liquid flowing out of the self-floating snow-squeezing module. It is preferred if the composition of the output of the device can conform to the composition of the crude oil output from the well. The composition of the synthetic crude oil output from the Fisher-阙 module can be varied by varying the temperature of the Fisher-Rich reactor and the composition of the syngas. The control system is configured to change the temperature of the Fisher-Rich reactor by varying the temperature of the fluid in the coolant passage and/or preheating the syngas prior to introduction of the Fisher- 阙 reactor. In addition, the composition of the synthetic crude oil is varied depending on the catalyst provided in the channel 706 of the Fisher-Tropsch reactor 40. In order to modify the percentage of different hydrocarbons in the synthetic crude oil, different catalysts can be used. Thus, the control system can be configured, for example, to recommend that in order to select the desired composition of the crude oil output from the device as a whole, it is desirable to replace the Fisher containing the catalyst with different catalysts when a Fisher-Dragon module has to be replaced.阙 module. The control system includes a performance monitoring system, and a plurality of valves configured to control various aspects of each of the reactors 24, 124, 40 and the device as a whole. The performance monitoring system measures the temperature of the fluid flowing through the modules and the device as a whole. 201006919 degrees, pressure, flow rate, and composition. The measured parameters are used to monitor short-term changes in the system, such as the reduction in available feed gas, which requires down-regulation of one or more modules. In addition, the measured parameters are used to observe long-term trends. A decrease in the CO and/or H2 content of the syngas, e.g., a temperature increase, or a fluid output that forms a vapor methane recombination reactor at a particular input temperature, indicates catalyst degradation within the reactor and may require regeneration or replacement. Since the unit contains a plurality of modules operating in parallel, the initial adjustment of the Fisher-Tropsch catalyst, or the reconstitution of the vapor methane recombination or the Fisher-catalyst catalyst can be carried out in the same place as the rest of the plant. Where applicable, catalyst reduction can be performed using HUs from other modules operating. Because of the complexity of this system, it uses model-based diagnostics as part of a performance monitoring system. Record the input parameters of each module or system component and input the model of the system's predicted ideal output parameters for each input parameter, and this.  The model compares the actual data of the device. Regarding the cause of the change between the two sets of data, the nature of the difference between the model data and the device data can be valuable. BRIEF DESCRIPTION OF THE DRAWINGS The present invention will now be further and more specifically described by way of example only with reference to the accompanying drawings in which: FIG. 1 is a diagrammatic representation of a typical variation of the associated gas flow rate over time in an oil producing facility, and Gas flow requirements of conventional GTL devices; Figure 2 graphically shows typical variations in productivity over time with or without the oil producing facility of the present invention; Figure 3 shows a processing device for carrying out the method of the present invention Flowchart of the example; -53- 201006919 Figure 4 shows a flow chart of another example of a processing device for carrying out the method of the invention; Figures 5A to 5H are schematic views of some different examples of the module; 6D is a schematic representation of some different examples of devices produced by the combination of modules of Figure 5; and Figures 7A and 7B show cross-sections of a portion of the reactors of the two examples. [Main component symbol description] 10 processing device

11 Separator 12 Crude oil 13 Associated gas 14 Oil storage tank 15 Washing 16 Mercury removal 17 Heat exchanger 18 Sulfur removal 20 Second heat exchanger 22 Front recombiner 24 Syngas generation reactor 26 Dotted line 30 Heat exchanger 31 Dotted line 32 compression stage 33 removed -54· 201006919

36 Yfii Ganzheng 38 Membrane Single 40 Fisher 4 Temperature 46 Heat 48 Separation 50 Synthesis 52 Membrane Single 55 Close 70 Stage 76 Preheat 99 Manifold 123 Preheat 124 Synthetic 126 Dot 500A Device 500B Device 501 Module 502 Mold Group 503 Module 504 Module 505 Synthesis 506 GTL 507 Syngas Generation Module Module Gas Generation Module Nickel Well Element - 阙 Synthesis Reactor Control System Converter Assembly Element Valve Interval Treatment Reactor Gas Generation Reactor Line - 55- .201006919 508 509 510 600 60 1 702 704 705 Ο 706 708 709 712 • C5 + . Ρ A Β

❿ C

D

G

V

T

R Syngas generation module Fisher-阙 module module auxiliary module manifold flat plate forming plate fin first flow channel second flow channel forming plate fin height hydrocarbon productivity initial increase plateau period gradually decreasing dotted line production rate flow rate time gas supply -56-

Claims (1)

201006919 X. Patent Application Range: 1. A device for treating natural gas comprising two or more modules connected in parallel; wherein the device is configured to convert the associated gas into a denser material. 2. For the device of claim 1 of the patent scope, at least one of the modules is a power module. 3. The apparatus of claim 1 or 2, wherein each module comprises two or more reactors connected in series or in parallel or a combination thereof. </ RTI> A device according to any of the above claims, wherein two or more modules are syngas generating modules containing one or more syngas generating reactors, and two or more modules are included Snow-阙 module for snow-阙 reactor. 5. The apparatus of claim 4, wherein all of the syngas generating molds are arranged in parallel; and all of the Fisher-阙 modules are arranged in parallel. - 6. The apparatus of claim 4, wherein the output of the plurality of syngas generating modules is connected to a common output manifold. 7. A device as claimed in any of the above claims, wherein at least one redundant module is provided under normal operating conditions ® . 8. An apparatus for treating natural gas, the apparatus comprising: a manufacturing conduit for connecting an oil well to extract oil and associated gas; and a processing unit configured to support: means for storing the extracted oil; and applying The device of any one of claims 1 to 7. 9. A method of treating associated gases of one or more wells, the method comprising the steps of: -57- 201006919 providing a modular device comprising two or more parallel modules, wherein at least one of the modules is a powerful module And at least one module is an economic module; one or more modules are down-regulated when productivity is reduced; and at least one or more modules are turned off when productivity drops below a downward limit. 10. If the method of claim 9 is applied, if the productivity is reduced to short-term, the closed module is a powerful module. 11. The method of claim 9 or 10, further comprising the step of shutting down a module when the flow of the associated gas drops below a predetermined lower limit for more than a predetermined time. 12. If the method of claim 11 is applied, the module that is closed is an economic module. 13. The method of any one of claims 9 to 11, wherein the modularizing device is configured to convert the associated gas into a liquid hydrocarbon, and wherein the liquid hydrocarbon is combined with the oil from the oil well. A control system which operates according to the method of any one of claims 9 to 13 of the patent application, as claimed in claim 1 to claim 8. ® 15. The control system of claim 14 further comprising means for monitoring the composition of the synthetic crude oil leaving the Fisher-Tropsch reactor, and for conforming or supplementing the output composition to the oil from the well The composition of the means to modify the conditions within the Fisher-阙 reactor. -58-