WO2018115596A1 - Procédé et système de fabrication de méthanol à partir de déchets organiques - Google Patents

Procédé et système de fabrication de méthanol à partir de déchets organiques Download PDF

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WO2018115596A1
WO2018115596A1 PCT/FI2017/050935 FI2017050935W WO2018115596A1 WO 2018115596 A1 WO2018115596 A1 WO 2018115596A1 FI 2017050935 W FI2017050935 W FI 2017050935W WO 2018115596 A1 WO2018115596 A1 WO 2018115596A1
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reactor
syngas
methanol
spiral
methanol synthesis
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PCT/FI2017/050935
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English (en)
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Mika RAUTIANEN
Annimari LEHTOMÄKI
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Avefori Oy
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Publication of WO2018115596A1 publication Critical patent/WO2018115596A1/fr

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    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
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Definitions

  • the invention relates to a method for manufacturing methanol from organic waste, wherein
  • syngas containing carbon monoxide, carbon dioxide and hydrogen in a syngas reactor applying a high temperature and pressure required by the manufacture of syngas
  • An object of the invention is also a corresponding system.
  • a problem related to efficient utilisation of biowaste has been to find a cost-efficient process for processes that produce a valuable end product.
  • Various prior art processes are known for producing biogas, for example, from waste.
  • One such process is proposed in the applicant's patent FI 125284 B.
  • a problem is the value of biogas produced, which is lower than that of further processed end products.
  • the well-known methanol synthesis process can be used for further processing.
  • a problem that arises here is related to the costs of further processing of biogas, which have traditionally been too high.
  • methanol synthesis In methanol synthesis, a traditional fixed bed reactor or a suspension reactor is used to manufacture methanol from syngas, wherein inadequate heat transfer and poor yield raise a problem. In this type of methanol synthesis reactors, due to the large cross-sectional flow area, syngas may pass through the methanol synthesis reactor without contacting the catalyst, in which case methanol is not generated or the yield remains low.
  • the object of the invention is to provide a method with a higher overall economic advantage compared to prior art methods for manufacturing methanol from organic waste.
  • the characteristic features of this invention are set forth in the appended claim 1.
  • Another object of the invention is to provide a system that is more advantageous than prior art systems for manufacturing methanol from organic waste.
  • the characteristic features of this invention are set forth in the appended claim 9.
  • the object of the method according to the invention can be achieved with a method for manufacturing methanol from organic waste, wherein biogas is produced from organic waste in a biogas reactor via anaerobic digestion, biogas is enriched using concentration equipment, and syngas containing carbon monoxide, carbon dioxide and hydrogen is produced in a syngas reactor . Further in the method, the temperature of syngas is decreased with a syngas cooler, syngas is condensed with a first condenser for separating excess water from syngas, and methanol is produced from syngas in a methanol synthesis reactor utilising a methanol synthesis catalyst .
  • the method uses a spiral reactor, wherein a reaction volume arranged from a pipe in a spiral form is used, with a catalyst arranged in this reaction volume in the methanol synthesis reactor. Furthermore in the method, the temperature of manufactured methanol is decreased with a methanol cooler andmixed gas is condensed in a second condenser for separating carbon dioxide and hydrogen of methanol from methanol.
  • a methanol synthesis reactor is advantageous as a spiral reactor in terms of manufacture regarding its investment costs.
  • a spiral reactor can be used without expensive tests related to the pressure vessel regulation, the pipe automatically meeting the regulations.
  • a pipe bent in a spiral form has a large specific surface area enabling efficient heat transfer.
  • the cross-sectional flow area of a spiral reactor is notably small compared, for instance, to large fixed bed reactors enabling syngas to efficiently collide with the catalyst in the reaction volume thus increasing the yield of the method. In this way, a method with low investment costs and a high yield is achieved.
  • the catalyst used in methanol synthesis is solid.
  • the catalyst can be easily kept inside the spiral reactor.
  • a solid catalyst can be allowed to gradually flow out from the spiral reactor for changing the catalyst.
  • biogas is purified before enriching it for removing hydrogen sulphide (H2S) and siloxanes. It is desirable to remove these substances, since they are known to lead to catalyst damage in the methanol synthesis reaction.
  • the method uses a spiral reactor as the syngas reactor for manufacturing syngas from water steam as steam reforming.
  • Steam reforming is a prior art method and thus quite well known.
  • the method uses a spiral reactor as the syngas reactor for manufacturing syngas with the partial oxidation method (POX) from methane and oxygen applying high temperature and pressure required by the partial oxidation method.
  • POX partial oxidation method
  • An advantage of using the partial oxidation method over steam reforming is the exothermic nature of partial oxidation reactions, enabling recovery of heat from the reactions.
  • the partial oxidation method consumes methane thus reducing the yield.
  • the method uses waste, which includes both organic fraction and inorganic fraction, of which inorganic waste can be burnt in a combustion boiler for producing at least heat .
  • waste which includes both organic fraction and inorganic fraction, of which inorganic waste can be burnt in a combustion boiler for producing at least heat .
  • Utilisation of heat recovered from the combustion of inorganic waste for heating methanol synthesis reduces the need of expensive external energy improving the economy of the process.
  • valuable methanol can be produced from invaluable raw material simultaneously also improving waste treatment from the environmental point of view, since waste can be exploited fully or at least mainly.
  • the syngas reactor is also a spiral reactor.
  • cost advantages are achieved when both the syngas reactor and the methanol synthesis reactor can have a similar basic design.
  • heat generating in the combustion boiler from the combustion of inorganic waste is used for preheating the steam reforming reactor by means of first heating equipment .
  • first heating equipment the energy content of inorganic waste can be efficiently utilised in endothermic reactions included in the manufacture of methanol.
  • Heat generating in the combustion boiler from the combustion of inorganic waste can also be used by means of second heating equipment for preheating the methanol synthesis reactor.
  • Spiral reactors are also advantageously used in the method as both the syngas cooler and the methanol cooler .
  • serial production for reactors and coolers which reduces the manufacturing costs of an individual spiral reactor and thereby improves the economy of the entire method.
  • this allows efficient utilisation of thermal energy provided by cooling for the preheating of the mixture supplied.
  • the method advantageously uses a pipe composed of two nested pipes made of different materials as the pipe forming the reaction volume, where the inner material is corrosion resistant and the outer material is black iron, as well as induction heating for heating the pipe .
  • the syngas reactor it is possible to apply a temperature ranging between 750°C and 950°C, preferably between 800°C and 900°C, and a pressure ranging between 15 bar and 30 bar, preferably between 18 bar and 22 bar, when manufacturing syngas using steam reforming. At a sufficiently high temperature and pressure, equilibrium of the reaction can be directed, with a good yield, towards desired intermediate products, which will be used later in methanol synthesis in the methanol synthesis reactor.
  • POX partial oxidation method
  • the catalyst used in the partial oxidation method can be a metal catalyst (transition metal catalyst), such as cobalt, nickel, iridium, palladium, platinum, rhodium or ruthenium.
  • this catalyst is also solid.
  • a high temperature and pressure enables direction of reaction equilibrium towards a high percent yield for methanol.
  • biogas is enriched using pressure swing adsorption by means of concentration equipment.
  • pressure swing adsorption the ratio of carbon dioxide and methane can be suitably adjusted for methanol synthesis, in which case a separate shift reaction may not be necessary.
  • Biogas can be enriched with concentration equipment in such a way that biogas contains 75-80% of methane and 20-25% of carbon dioxide relative to the total mass of biogas.
  • methane and carbon dioxide have a correct ratio as regards methanol synthesis for achieving a yield as high as possible.
  • Hydrogen is advantageously used as a reagent in the syngas reactor when manufacturing syngas using steam reforming.
  • a catalyst for methanol synthesis one of the following can be used in a solid form: Cu, nO, AI2O3.
  • Syngas efficiently collides with a solid catalyst in a spiral with a small cross-sectional flow area thereby improving the yield.
  • Carbon dioxide separated in a second condenser can be recirculated back to the methanol synthesis reactor to provide a better yield. Since carbon dioxide is one of the raw materials of methanol synthesis, it is useful to recirculate the carbon dioxide remaining in the product stream that exits from methanol synthesis back to the methanol synthesis reactor as input, adjusting in this way the required carbon dioxide ratio.
  • the object of the system according to the invention can be achieved with a system for manufacturing methanol from organic waste, the system including a biogas reactor for producing biogas from organic waste via anaerobic digestion, concentration equipment for enriching biogas produced, and a syngas reactor for manufacturing syngas containing carbon monoxide, carbon dioxide and hydrogen at a high pressure and temperature required by the manufacture of syngas .
  • the system further includes a syngas cooler for decreasing the temperature of syngas, a first condenser for condensing syngas for separating excess water from syngas, and a methanol synthesis reactor for manufacturingmethanol from syngas by means of a methanol synthesis catalyst.
  • At least the methanol synthesis reactor is a spiral reactor, having a reaction volume arranged from a pipe in a spiral form and a catalyst fitted therein.
  • the system includes a methanol cooler for decreasing the temperature of methanol, as well as a second condenser for separating hydrogen and carbon dioxide contained in methanol from mixed gas. Due to the use of a spiral reactor, a system according to the invention is more advantageous in terms of its investment costs and provides better yield compared to prior art systems based on the criteria presented earlier in context with the method.
  • the syngas reactor is also a spiral reactor.
  • synergy is achieved in the manufacture of the system, as the basic solution for the structures of both the syngas reactor and the methanol synthesis is similar thus automatically meeting the requirements according to the pressure vessel standard.
  • the system includes a combustion boiler for burning inorganic waste to provide at least heat and preferably as well.
  • waste can be utilised in the process fully or at least mainly, and low-cost heat and electricity are available for the endothermic reactions related to methanol manufacture, which improves the total economy of the process.
  • the system may include separation equipment for separating waste used as input into organic and inorganic fraction.
  • separation equipment for separating waste used as input into organic and inorganic fraction.
  • waste can be sorted on site, and any mixed waste is suitable as raw material for methanol production.
  • the system includes heating equipment for preheating the syngas reactor utilising heat generated during the combustion of inorganic waste.
  • the system also includes second heating equipment for preheating the methanol synthesis reactor utilising heat generated during the combustion of inorganic waste.
  • Concentration equipment advantageously consists of pressure swing adsorption columns (PSA columns) .
  • PSA columns pressure swing adsorption columns
  • the ratio of carbon dioxide and methane can be adjusted suitable for methanol synthesis .
  • the use of PSA columns is easily scalable to provide a capacity that is suitable for the application .
  • the pipe of the spiral reactor is double layered, where the inner material of the pipe is made of a metal that protects from oxidation and corrosion while the outer material is a material enabling induction heating .
  • the inner material of the pipe is made of a metal that protects from oxidation and corrosion
  • the outer material is a material enabling induction heating .
  • the spiral reactor used as the syngas reactor and as the methanol synthesis reactor or as both of these includes induction coils as heat transfer equipment for heating the pipe with electric current .
  • induction With induction, the temperature of the spiral reactor can be efficiently increased to an adequately high value.
  • the spiral reactor includes a spiral reaction chamber constituting the reaction volume for raw materials, heat transfer equipment arranged outside the spiral reaction chamber for transferring heat between the raw material in the spiral reaction chamber and the heat transfer equipment, as well as feed equipment for supplying raw material to the spiral reaction chamber constituting the reaction volume.
  • the spiral reaction chamber is a tubular structure arranged in a spiral form.
  • a tubular structure arranged in a spiral form enables fitting a sufficiently long tubular structure in a small space.
  • a tubular structure has a strong construction and it resists to a high pressure, the reactor thus being particularly favourable in terms of manufacture.
  • the spiral reactor also includes feed equipment arranged to supply raw materials in such a way that raw materials have a stable flow in the spiral reaction chamber for preventing their separation.
  • the feed equipment provides an adequate flow speed in the reactor preventing the separation of intermediate products .
  • the feed equipment may consist of a pump.
  • the feed equipment may be arranged to supply raw material to the spiral reactor at a speed that allows a sufficient dwell time in the spiral reactor.
  • the supply speed must be selected so that the spiral reaction chamber has an adequate length in order to achieve the desired end result with the spiral reactor regardless of whether this is an end product of a reaction or heating or cooling of raw materials .
  • the spiral reaction chamber is a spiral pipe having such a length that the reaction rate of the raw material passing through is at least 95% over the reactor.
  • the diameter of the spiral reactor pipe is preferably between 10 mm and 80 mm.
  • a pipe with such a diameter can be bent reasonably easily and yet it offers a sufficient volume for providing the necessary capacity.
  • a specific pressure vessel permit is not required for an adequately thin pipe.
  • the wall thickness of the pipe is preferably between 1.0 mm and 10.0mm.
  • the pipe is sufficiently resistant in terms of pressure levels, yet easily formable in a spiral form.
  • the heat transfer equipment of the spiral reactor consists of a vessel fitted around a tubular structure and having a liquid or gaseous heat transfer medium within it. With the heat transfer medium, heat can be transferred from the reactor to the heat transfer medium using a separate heater and thereby to the spiral structure surrounded by the heat transfer medium and constituting the spiral reaction chamber.
  • a liquid heat transfer medium may be heat transfer oil. The caloric capacity of oil is high and thereby the heating capacity is high.
  • the heat transfer equipment of the spiral reactor consists of induction coils fitted around a tubular structure, arranged to heat the tubular structure made of black iron.
  • the heating efficiency may be higher than when using a heat transfer medium.
  • such a construction is more favourable in terms of manufacture compared to heat transfer equipment that utilises a heat transfer medium, and adjustment of the temperature is more accurate.
  • the spiral reactor advantageously includes a vessel or a casing arranged around the heating equipment and including an insulation layer for preventing heat transfer. Thus, heat used for heating the spiral reactor chamber cannot escape to the area surrounding the reactor.
  • the outer diameter of the spiral pipe may range between 0.5% and 20%, preferably between 0.5% and 5% of the outer diameter of the vessel , and the length of the vessel is between 1% and 10%, preferably less than 5% of the length of the spiral pipe.
  • outer dimensions of the vessel simultaneously also mean outer dimensions of an individual reactor.
  • the feed equipment included in the spiral reactor consists of a high-pressure pump.
  • a high-pressure pump it is possible to increase the pressure of the raw material to a desired state in order to carry out desired reactions.
  • the syngas cooler and the methanol cooler are also volumes arranged from a pipe in a spiral form. Due to the spiral, heat transfer is efficient and the coolers are advantageous in terms of manufacture.
  • the catalyst of the methanol synthesis reactor is preferably one of the following: Cu, nO, AI2O3, and the catalyst is solid and in one or more of the following forms: granules, pellets and/or rings.
  • a solid catalyst has a sufficiently large surface area in the reaction volume in order that the collision with syngas takes place without the catalyst blocking the spiral reactor.
  • the syngas reactor and the methanol synthesis reactor preferably formed from spirals, as well as the syngas cooler and the methanol cooler, also implemented as spirals, form a spiral reactor set.
  • a spiral reactor set is easy to implement due to similar structures and also advantageous to place in a movable unit, such as a transfer container .
  • the system advantageously includes a pipework for connecting a biogas reactor to concentration equipment, a second pipework for connecting the concentration equipment to a syngas reactor, a third pipework for connecting the syngas reactor to a syngas cooler, a fourth pipework for connecting the syngas cooler to a first condenser, a fifth pipework for connecting the first condenser to a methanol synthesis reactor, a sixth pipework for connecting the methanol synthesis reactor to a methanol cooler and a seventh pipework for connecting the methanol cooler to a second condenser.
  • the system advantageously includes pumps and valves for transferring and guiding material streams .
  • Figure 1 is a block diagram illustrating a system and a method according to the invention
  • Figure 2 is a basic view of a spiral reactor used as a methanol synthesis reactor in a system according to the invention
  • Figure 3 is a basic view of a tubular structure of a spiral reactor used as a cooler in a system according to the invention
  • Figure 4 is a partial cross-sectional view of an advantageous design of a spiral reactor pipe used in a system according to the invention .
  • various types of mixed waste can be used as raw material, such as Municipal Solid Waste (MSW) including both organic and inorganic waste with variable ratios.
  • Municipal Solid Waste MSW
  • Municipal Solid Waste Municipal Solid Waste
  • Municipal Solid Waste used as raw material in the method
  • prior art sorting equipment 11 can be used according to figure 1.
  • waste can be brought to the process already fractionated.
  • inorganic fraction is led to a combustion boiler 12 where it is burnt to produce at least heat. A portion of heat can also be used for electricity production in order to obtain electricity for the treatment of organic fraction without transmission charges from an external electricity network.
  • the combustion boiler 12 can be a prior art CHP (Combined Heat and Power Production) unit, for example, a fluidised bed boiler , a circulating fluidised bed boiler or an equivalent combustion boiler suitable for the application.
  • CHP Combined Heat and Power Production
  • biogas reactor 14 is advantageously a biogas reactor similar to that known from the FI patent 125284 B, where a biogas reactor of the plug flow reactor model is divided into several independently controllable blocks enabling maximisation of biogas production using anaerobic digestion.
  • the biogas reactor can also be another prior art biogas reactor with which it is possible to obtain biogas that contains at least methane and carbon dioxide as a product.
  • biogas or pyrolytic gas releasing from landfill sites can be utilised in the process.
  • Biogas recovered from the biogas reactor 14 contains approximately 50-75% by volume of methane (CH4) and the rest is mainly carbon dioxide (CO2) .
  • Biogas can be led to biogas purification 15, where hydrocarbons and siloxanes are removed, or directly to concentration equipment 16, where biogas is enriched for methanol synthesis using preferably pressure swing adsorption (PSA process ) to reach a suitable concentration ratio relative to methane and carbon dioxide.
  • PSA process pressure swing adsorption
  • other methods suitable for enrichment can also be used, such as membrane separation; however, pressure swing adsorption is easily scalable according to the required production capacity.
  • the ratio of methane and carbon dioxide can be easily adjusted suitable for methanol synthesis.
  • readings such as 75-80% of methane and 20-25% of carbon dioxide relative to the total biogas mass are aimed at.
  • the syngas reactor 18 is advantageously a spiral reactor 34, an embodiment of which is shown in figure 2.
  • the reaction volume 38 is constituted by a pipe 36 arranged in a spiral form.
  • the spiral reactor 34 includes three parts 35, of which two parts are preheating parts, wherein the pipe 36 is heated by means of a vessel 42 and a heat transfer medium 44.
  • the vessel 42 and the heat transfer medium 44 thus function as the first heating equipment 20 for preheating.
  • the third part is advantageously an induction heating part, where the pipe 36 is heated by means of induction coils 48.
  • induction heating Due to induction heating, it is possible to increase the temperature in the syngas reactor to an adequately high value, since heat recovered from the combustion boiler is insufficient to adequately shift reaction equilibrium to the end product side to provide a high syngas yield.
  • syngas when speaking of syngas, a mixture of carbon monoxide, carbon dioxide and hydrogen is meant.
  • An advantage of the partial oxidation method is that the reactions are exothermic, which allows the use of recovered heat for preheating the methanol synthesis reactor, for example.
  • the partial oxidation method and gas reforming can also be used in parallel, if two syngas reactors are used in parallel.
  • gas reforming and the partial oxidation method can be used as methods alternative to each other for manufacturing syngas; on the other hand, they can also be used in parallel.
  • spiral reactor is shown on its own in figure 2, it is obvious to those skilled in the art that, for example, components 35 used for preheating, forming part of the spiral reactor 34 may be integrated into the vicinity of the combustion boiler.
  • a syngas cooler 22 which is also preferably a spiral reactor .
  • a vessel 42 containing heat transfer medium 44 may be disposed around the pipe 36 bent in a spiral form, according to figure 3. With the heat transfer medium, heat can be transferred from the discharge stream of the syngas reactor 18 to be used for preheating the methanol synthesis reactor 26, for example.
  • the heat transfer medium 44 can be cooled with a separate heat exchanger, for example.
  • the cooled volume flow of carbon monoxide, carbon dioxide and hydrogen is led from the syngas cooler to the first condenser 24 at a temperature of approximately 65°C.
  • water remained in the volume flow is removed and can be recirculated back to the syngas reactor inlet.
  • Both the first condenser 24 and the second condenser 32 can be completely prior art condensers.
  • the volume flow of carbon monoxide, carbon dioxide and hydrogen can be led from the first condenser to a separate shift reactor, by means of which it is possible to adjust, if necessary, the ratio of carbon dioxide and hydrogen suitable as regards methanol synthesis.
  • the reaction taking place in the shift reactor is as follows:
  • a shift reactor is not absolutely necessary, if concentration equipment based on pressure swing adsorption is used as concentration equipment, since the ratio of carbon dioxide and hydrogen can be adjusted during enrichment with pressure swing adsorption .
  • concentration equipment based on pressure swing adsorption
  • the ratio of carbon dioxide and hydrogen can be adjusted during enrichment with pressure swing adsorption .
  • the reaction mixture of carbon monoxide, carbon dioxide and hydrogen is led to a methanol synthesis reactor 26, which, according to the invention, is a spiral reactor 34.
  • the design of the spiral reactor 34 used as the methanol synthesis reactor 26 can be corresponding to that shown in figure 2.
  • the second heating equipment 28 associated with the spiral reactor 34 can also consist of a vessel 42 and heat transfer medium 44, by means of which heat provided by the combustion boiler can be utilised for preheating.
  • the spiral reactor may also include a third part with induction heating, which is used to provide the final reaction temperature.
  • the methanol synthesis reactor can have between 2 and 5 stages, where cooler inlet gas can be supplied to the various stages for controlling the reaction temperature.
  • the methanol synthesis reactor 26 it is possible to apply a temperature ranging between 250°C and 450°C, preferably between 300°C and 400°C and a pressure ranging between 40 bar and 120 bar, preferably between 50 bar and 100 bar.
  • a temperature ranging between 250°C and 450°C preferably between 300°C and 400°C
  • a pressure ranging between 40 bar and 120 bar preferably between 50 bar and 100 bar.
  • the product stream discharged from the methanol synthesis reactor 26 containing methanol, water, carbon dioxide and hydrogen is led to a methanol cooler 30, which can be a spiral reactor 34 corresponding to the syngas cooler 22.
  • the temperature of the product stream is advantageously decreased in the spiral reactor, which enables the recovery and utilisation of the heat energy contained in the product stream .
  • the cooled product stream is led to a second cooler 32 , where methanol and water are condensed and separated from gaseous carbon dioxide and hydrogen.
  • carbon dioxide and hydrogen can be led back to the methanol synthesis reactor 26, whereas methanol and water can be led to storage or they can be separated from each other in a distillation column, for example.
  • the evenly spaced dashed lines refer to transferrable heat
  • the dashed lines from the second condenser 32 to the methanol synthesis reactor 26 refer to the recyclable carbon dioxide.
  • the spiral reactor 34 used as the methanol synthesis reactor and possibly also as the syngas reactor may consist of several parts 35, of which each part is an individual spiral reactor 34. These parts 35 differ from each other by the heat transfer equipment 40 included in the spiral reactor 34, which can consist, for example, of the vessel 42 in the first and the second spiral reactor 34, as depicted in the figure, and the heat transfer medium 44 surrounding the pipe 36 arranged within it in a spiral form.
  • the heat transfer equipment 40 included in the spiral reactor 34 can consist, for example, of the vessel 42 in the first and the second spiral reactor 34, as depicted in the figure, and the heat transfer medium 44 surrounding the pipe 36 arranged within it in a spiral form.
  • Such an embodiment of the spiral reactor 34 is also shown in figure 3.
  • this type of spiral reactor can be used as a syngas cooler 22 or a methanol cooler 28 or both in a system 10 according to the invention .
  • the diameter of the vessel constituting the casing can be 210 mm, for example.
  • the vessel can also be different from the cylinder of figure 1, such as a sphere.
  • a sphere In this embodiment, approximately 60 m of pipe 36 having an outer diameter of 20 mm and a wall thickness of 2 mm, for example, is placed inside the vessel 42.
  • the heat transfer medium is advantageously heat transfer oil.
  • the heat transfer medium such as heat transfer oil
  • the heat transfer medium can alternatively be cooled for cooling purposes with a heat exchanger, for example, or heated for heating purposes with electrical resistances, for example, or with an exhaust gas heat exchanger of a combustion boiler for inorganic waste, in the circulation furnace of a circulating fluidised bed boiler or in the furnace of a fluidised bed boiler, where the heat transfer oil can be heated even to a temperature exceeding 400°C.
  • the reactor vessel is made tight in such a way that it keeps the heat transfer medium inside it and is simultaneously insulated in such a way that escape of heat out from the vessel is prevented.
  • the third part 35 in figure 2 is the second embodiment of the spiral reactor 34, which differs from the embodiment of figure 3 for the heat transfer equipment 40.
  • the heating of the reaction mixture takes place by heating a pipe 36 with induction coils 48, which constitute the heat transfer equipment 40.
  • the induction coils 48 are placed around the pipe that forms a tubular structure, and alternating current led to these generates a variable magnetic field inside the induction coils 48, the magnetic field inducing inside the induction coils 48 turbulent flows that heat the tubular structure.
  • the pipe 36 is made of black iron, which has a particularly high resistance and thus it warms up particularly efficiently due to electricity.
  • the output of induction coils can be in a class of 200 to 500 kW over a reactor containing a pipe with a length of 60 m and placed in a spiral.
  • the spiral reaction chamber is advantageously isolated from the environment by means of a vessel 42.
  • the vessel 42 is heat insulating, preventing, at the same time, the electrical field from shifting outside the reactor .
  • the pipe 36 used as the reaction volume in the spiral reactor 34 is a double layer pipe, where the inner material 50 is more precious metal for preventing corrosion and the outer material 52 is carbon steel, for example.
  • the thickness of the inner surface layer is advantageously only between 0.2 and 0.6 millimetres for saving material costs.
  • a double layer pipe can be manufactured in such a way that precision steel pipes are mechanically installed within each other before the manufacture of the spiral reactor .
  • the more precious metal of the inner material 50 can be, for example, chromium or similar, which resists to the supercritical conditions prevailing in a spiral reaction chamber.
  • the catalyst 1 can be placed over the entire length of the pipe 36, as shown in figure 4 with a dashed line.
  • the capacity of the spiral reactor can be such that raw material is supplied at 6 to 10 L/min to the reactor , into a spiral reaction chamber manufactured f om a pipe with an inside diameter of 18 mm and a total length of 360 m.
  • the flow speed is between 0.39 and 0.63 m/s and the total volume of the reactor is approximately 92 L .
  • the spiral reactor is advantageously scalable to achieve higher production capacities using spiral reactors in parallel or in series or both of these .
  • the system advantageously includes , as shown in the figure 1 , a first pipework 100 for connecting a biogas reactor 14 to concentration equipment 16 , a second pipework 102 for connecting the concentration equipment 16 to a syngas reactor 18 , a third pipework 104 for connecting the syngas reactor 18 to a syngas cooler 22 , a fourth pipework 106 for connecting the syngas cooler to a first condenser 2 4 , a fifth pipework 108 for connecting the first condenser 24 to a methanol synthesis reactor 26, a sixth pipework 110 for connecting the methanol synthesis reactor 26 to a methanol cooler 30 and a seventh pipework 112 for connecting the methanol cooler to a second condenser 32.

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Abstract

L'invention concerne un procédé de fabrication de méthanol à partir de déchets organiques comprenant les étapes consistant à produire un biogaz à partir de déchets organiques dans un réacteur de biogaz (14) par digestion anaérobie, enrichir le biogaz, produire un gaz de synthèse dans un réacteur de gaz de synthèse (18), réduire la température du gaz de synthèse avec un refroidisseur de gaz de synthèse (22), condenser le gaz de synthèse pour séparer l'excès d'eau du gaz de synthèse, produire du méthanol dans un réacteur de synthèse de méthanol (26) à l'aide d'un catalyseur de synthèse de méthanol, réduire la température du méthanol fabriqué avec un refroidisseur de méthanol (30), condenser le gaz mélangé dans un second condenseur (32) pour séparer le dioxyde de carbone et l'hydrogène de méthanol du méthanol. Au moins en tant que réacteur de synthèse de méthanol (26), le procédé utilise un réacteur en spirale (34), utilisant un volume de réaction (38) agencé à partir d'un tuyau (36) en forme de spirale, avec un catalyseur disposé dans ce volume de réaction (38). L'invention concerne aussi un système correspondant.
PCT/FI2017/050935 2016-12-23 2017-12-27 Procédé et système de fabrication de méthanol à partir de déchets organiques WO2018115596A1 (fr)

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FI20166030A FI20166030L (fi) 2016-12-23 2016-12-23 Menetelmä ja järjestelmä metanolin valmistamiseksi orgaanisesta jätteestä
FI20166030 2016-12-23

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111960920A (zh) * 2020-08-17 2020-11-20 中国神华煤制油化工有限公司 用于davy甲醇合成装置的物料回收设备以及物料回收方法
WO2020254121A1 (fr) * 2019-06-18 2020-12-24 Haldor Topsøe A/S Valorisation de biogaz en méthanol

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US5266281A (en) * 1989-09-16 1993-11-30 Xytel Technologies Partnership Catalytic reactor
EP1008577A1 (fr) * 1998-12-07 2000-06-14 Mitsubishi Heavy Industries, Ltd. Procédé pour la préparation de méthanol
WO2015086904A1 (fr) * 2013-12-11 2015-06-18 Biogts Oy Procédé et système de production de biocarburant liquide provenant d'huiles et/ou de graisses à base biologique
WO2016179476A1 (fr) * 2015-05-06 2016-11-10 Maverick Biofuels, Inc. Digesteur anaérobie et système gtl combinés et procédé d'utilisation de ceux-ci

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5266281A (en) * 1989-09-16 1993-11-30 Xytel Technologies Partnership Catalytic reactor
EP1008577A1 (fr) * 1998-12-07 2000-06-14 Mitsubishi Heavy Industries, Ltd. Procédé pour la préparation de méthanol
WO2015086904A1 (fr) * 2013-12-11 2015-06-18 Biogts Oy Procédé et système de production de biocarburant liquide provenant d'huiles et/ou de graisses à base biologique
WO2016179476A1 (fr) * 2015-05-06 2016-11-10 Maverick Biofuels, Inc. Digesteur anaérobie et système gtl combinés et procédé d'utilisation de ceux-ci

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020254121A1 (fr) * 2019-06-18 2020-12-24 Haldor Topsøe A/S Valorisation de biogaz en méthanol
CN113993811A (zh) * 2019-06-18 2022-01-28 托普索公司 沼气升级为甲醇
CN111960920A (zh) * 2020-08-17 2020-11-20 中国神华煤制油化工有限公司 用于davy甲醇合成装置的物料回收设备以及物料回收方法
CN111960920B (zh) * 2020-08-17 2023-01-13 中国神华煤制油化工有限公司 用于davy甲醇合成装置的物料回收设备以及物料回收方法

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