A high pressure fluidized bed reactor, recycle system and method for the synthesis of aromatics from synthesis gas

Abstract

The application provides a high-pressure fluidized bed reactor for preparing aromatics from synthesis gas, wherein a wind distribution plate, an inner component and an inner cyclone separator are sequentially arranged in the chamber of the fluidized bed reactor along the gas flow direction, and a turbulence component and a flow guide plate are arranged to effectively strengthen the gas-solid heat and mass transfer in the reactor, and the turbulence component has a cooling liquid channel inside, so that the temperature distribution uniformity of the reaction area is ensured during the reaction process of preparing aromatics from synthesis gas, and the high-pressure fluidized bed reactor has high mass and heat transfer efficiency, so that the synthesis gas is efficiently converted into aromatics. The application also provides a circulation system for preparing aromatics from synthesis gas, which comprises the high-pressure fluidized bed reactor, and adopts a circulating gas supply mode to further improve the conversion rate of synthesis gas and the yield of aromatics. The circulation system for preparing aromatics from synthesis gas has simple equipment structure and short process flow, and has great potential in the application of important chemical technologies such as one-step aromatics preparation.

Description

Technical Field

[0001] This invention relates to the field of syngas-to-aromatics technology, and more particularly to a high-pressure fluidized bed reactor, circulation system and method for syngas-to-aromatics production. Background Technology

[0002] Aromatics are important bulk organic chemical raw materials, mainly used in the production of various polymers such as nylon, polyester, resins, polyurethane, and films. Globally, over 70% of light aromatics (BTX) are produced through naphtha reforming. With the continued shortage of petroleum resources and my country's energy structure characterized by "abundant coal, scarce gas, and poor oil," there is an urgent need to develop new non-petroleum-based aromatics production technologies. Coal-to-aromatics can reduce the dependence of traditional processes on petroleum resources.

[0003] Traditional Fischer-Tropsch synthesis products follow the ASF rule, exhibiting low selectivity for aromatics. Researchers have been striving to explore a route for aromatics production that breaks the ASF rule. In the late 1970s, Mobil proposed two technical routes for aromatics production from syngas: coal-syngas-methanol-aromatics (MTA) and one-step coal-syngas-aromatics production (STA).

[0004] Compared to the traditional MTA process, the STA process (oxygen-containing compound intermediate route) has the advantage of reduced equipment investment and operating costs. If it can meet requirements such as high CO conversion rate, good catalyst stability, narrow aromatic product distribution, and high-value-added aromatic byproducts, it will have even more considerable economic benefits. The one-step syngas-to-aromatics (STA) process has advantages such as a short route and low equipment investment, making it a promising technical route with broad application prospects.

[0005] In the development of catalysts for one-step synthesis of aromatics from syngas, the composition of metal oxides, the bimetallic ratio, crystal form and grain size, the ratio of oxides to molecular sieves, and the physicochemical properties of molecular sieves such as acidity and diffusivity have a significant impact on reaction performance. Currently, the CO conversion rate of the one-step synthesis of aromatics from syngas can reach 20%–50%, and the aromatic selectivity can reach 50%–80%. However, key issues that still need to be addressed include low CO conversion rate, low space-time yield of aromatics, temperature matching of bifunctional catalysts, long-term stability of catalysts, and catalyst regenerability. Summary of the Invention

[0006] To address the aforementioned problems in the existing technology, this invention provides a high-pressure fluidized bed reactor, circulation system, and method for producing aromatics from syngas, thereby further improving the CO conversion rate in the one-step syngas-to-aromatics reaction process.

[0007] The specific details of the invention are as follows:

[0008] In a first aspect, the present invention provides a high-pressure fluidized bed reactor for producing aromatics from syngas, wherein the fluidized bed reactor is provided with an air distribution plate, internal components and a built-in cyclone separator arranged sequentially along the gas flow direction in the chamber of the fluidized bed reactor.

[0009] The air distribution plate is a metal air distribution plate with nozzle-type channels distributed thereon, and the total area of ​​the nozzle-type channels accounts for 3% to 10% of the area of ​​the air distribution plate; the mesh size of the air distribution plate in other areas besides the nozzle-type channels is 200 to 500 mesh.

[0010] The internal components are composed of spaced-out baffles and guide vanes, and the total number of layers is an odd number. The first layer of the internal components on the side closest to the air distribution plate is the baffle.

[0011] Optionally, the turbulence-disrupting element is in the shape of a water droplet and / or a cylinder; the guide plate is in the shape of a rhombus or a triangle.

[0012] Optionally, the spoiler has a coolant channel inside.

[0013] Optionally, the gas-solid inlet channel of the built-in cyclone separator is provided with an inverted triangular inertial baffle, which is arranged in two staggered rows for the initial separation of larger solid particles.

[0014] The gas outlet of the built-in cyclone separator is equipped with a corrugated filter screen for further separation of catalyst fine powder.

[0015] Secondly, the present invention provides a circulating system for producing aromatics from syngas, comprising: the high-pressure fluidized bed reactor described in the first aspect, and a fractionation tower, a separating tank, a washing tank, a circulating pressurization pump, a mixing tank, and a preheating furnace; wherein...

[0016] The outlet of the high-pressure fluidized bed reactor is connected to the inlet of the fractionation tower, which is used to fractionate the mixed gas 1 containing aromatic products discharged from the outlet of the high-pressure fluidized bed reactor to obtain liquid aromatic products.

[0017] The gas outlet at the top of the fractionation tower is connected to the inlet of the liquid separator, which is used to further remove the liquid component from the mixed gas 2 discharged from the gas outlet of the fractionation tower.

[0018] The gas outlet of the separator is connected to the inlet of the water washing tank, and the water washing tank is used to remove impurities from the mixed gas 3 discharged from the gas outlet of the separator.

[0019] The outlet of the washing tank is connected to the inlet of the circulating pressurizing pump, which is used to pressurize the mixed gas 4 discharged from the outlet of the washing tank.

[0020] The outlet of the circulating pressurizing pump is connected to the inlet of the mixing tank, and the mixing tank is used to mix the mixed gas 4 discharged from the outlet of the circulating pressurizing pump with the raw material synthesis gas;

[0021] The outlet of the mixing tank is connected to the inlet of the preheating furnace, and the preheating furnace is used to heat the mixed gas 5 discharged from the outlet of the mixing tank;

[0022] The outlet of the preheating furnace is connected to the feed gas inlet of the high-pressure fluidized bed reactor. The high-pressure fluidized bed reactor uses the mixed gas 5 discharged from the outlet of the preheating furnace as the reaction feedstock and obtains aromatic products under the action of a bifunctional catalyst.

[0023] Optionally, the fractionation tower is provided with a liquid outlet at the bottom, which is connected to a liquid collection tank for collecting the liquid aromatic products accumulated at the bottom of the fractionation tower.

[0024] Thirdly, the present invention provides a syngas-to-aromatics recycling system, the method being applicable to the syngas-to-aromatics recycling system described in the second aspect above, the method comprising:

[0025] S1. Load a bimetallic catalyst into a high-pressure fluidized bed reactor and introduce syngas into the high-pressure fluidized bed reactor. Under the action of the bifunctional catalyst, the syngas yields aromatic products.

[0026] S2. The mixed gas 1 containing aromatic products is discharged from the outlet of the high-pressure fluidized bed reactor and introduced through the inlet of the fractionation tower to fractionate the mixed gas and obtain liquid aromatic products.

[0027] S3. The remaining mixed gas 2 after fractionation is discharged from the gas outlet at the top of the fractionation tower and introduced through the inlet of the liquid separator to further remove the liquid components in the mixed gas 2.

[0028] S4. The remaining mixed gas 3 after removing the liquid components is discharged from the gas outlet of the separator and introduced through the inlet of the water washing tank to remove impurities in the mixed gas 3.

[0029] S5. The remaining mixed gas 4 after removing impurities is discharged from the outlet of the water washing tank and introduced through the inlet of the circulating pressurization pump to pressurize the mixed gas 4.

[0030] S6. The pressurized mixed gas 4 is discharged from the outlet of the circulating pressurization pump and introduced through the inlet of the mixing tank to mix the raw material synthesis gas and mixed gas 4 to obtain mixed gas 5.

[0031] S7. Discharge the mixed gas 5 from the outlet of the mixing tank and introduce it through the inlet of the preheating furnace to heat the mixed gas 5;

[0032] S8. The heated mixed gas 5 is discharged from the outlet of the preheating furnace and introduced into the feed gas inlet of the high-pressure fluidized bed reactor. Under the action of the bifunctional catalyst, aromatic products are obtained.

[0033] Optionally, the temperature inside the high-pressure fluidized bed reactor is 250–550°C, and the pressure is 2 MPa–6 MPa.

[0034] The distillation tower operates at a pressure of 2 MPa to 6 MPa.

[0035] Optionally, the particle size of the bifunctional catalyst is 50-150 μm, and the loading of the bifunctional catalyst is 3-5 times the height-to-diameter ratio of the high-pressure fluidized bed reactor.

[0036] Optionally, the volume ratio of CO to H2 in the synthesis gas is 1:1 to 1:1;

[0037] The circulation ratio of the mixed gas 4 is 2.5 to 6.

[0038] Compared with the prior art, the present invention has the following advantages:

[0039] This invention provides a high-pressure fluidized bed reactor for the preparation of aromatics from syngas. The fluidized bed reactor has an air distribution plate, internal components, and a built-in cyclone separator arranged sequentially along the gas flow direction in its chamber. The arrangement of the turbulence components and the guide plate effectively enhances the gas-solid heat and mass transfer within the reactor. Furthermore, the turbulence components have cooling liquid channels inside, ensuring the uniformity of temperature distribution in the reaction zone during the preparation of aromatics from syngas. This results in a high-pressure fluidized bed reactor with high mass and heat transfer efficiency, thereby ensuring the efficient conversion of syngas into aromatics.

[0040] This invention also provides a circulating system and method for preparing aromatics from syngas. Based on the aforementioned high-pressure fluidized bed reactor, this system incorporates a fractionation tower, a separator, a washing tank, a circulating pressurization pump, a mixing tank, and a preheating furnace. Employing a circulating gas supply method, it further improves the syngas conversion rate and aromatics yield. The circulating system for preparing aromatics from syngas provided by this invention has a simple equipment structure and a short process flow, demonstrating great potential for applications in important chemical technologies such as one-step aromatics production. Attached Figure Description

[0041] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0042] Figure 1A schematic diagram of the high-pressure fluidized bed reactor for producing aromatics from syngas provided in an embodiment of the present invention is shown.

[0043] Figure 2 A partial schematic diagram of the high-pressure fluidized bed reactor for producing aromatics from syngas provided in an embodiment of the present invention is shown.

[0044] Figure 3 A schematic diagram of the built-in cyclone separator provided in an embodiment of the present invention is shown;

[0045] Figure 4 A schematic diagram of the syngas-to-aromatics cycle system provided in an embodiment of the present invention is shown.

[0046] Figure 5 A flowchart of a method for producing aromatics from syngas according to an embodiment of the present invention is shown.

[0047] Explanation of reference numerals in the attached figures:

[0048] 1-High-pressure fluidized bed reactor, 2-Fracturing tower, 3-Separating tank, 4-Washing tank, 5-Circulating pressurization pump, 6-Mixing tank, 7-Preheating furnace, 8-Collection tank, 101-Air distribution plate, 1011-Nozzle-type channel, 102-Internal components, 1021-Break-off component, 1022-Guide plate, 103-Built-in cyclone separator, 1031-Inertial baffle, 1032-Corrugated filter screen. Detailed Implementation

[0049] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The following description of at least one exemplary embodiment is merely illustrative and is in no way intended to limit the present invention or its application or use. Based on the embodiments of the present invention, any product that is the same as or similar to the present invention, derived by any person under the guidance of the present invention or by combining the features of the present invention with other prior art, falls within the protection scope of the present invention. Furthermore, all other embodiments obtained by those skilled in the art without inventive effort are within the protection scope of the present invention.

[0050] Specific experimental steps or conditions are not specified in the embodiments; they can be performed according to the conventional experimental steps or conditions described in the prior art. Reagents and other instruments used, unless otherwise specified, are all commercially available conventional reagent products. Furthermore, the accompanying drawings are merely illustrative diagrams of the embodiments of the present invention and are not necessarily drawn to scale. The same reference numerals in the drawings denote the same or similar parts, and therefore, repeated descriptions of them will be omitted. Some block diagrams shown in the drawings are functional entities and do not necessarily correspond to physically or logically independent entities.

[0051] Techniques, methods, and equipment known to those skilled in the art may not be discussed in detail, but where appropriate, such techniques, methods, and equipment should be considered part of the specification.

[0052] In the description of this invention, it should be understood that the use of terms such as "first" and "second" to define components is merely for the purpose of distinguishing the corresponding components. Unless otherwise stated, the above terms have no special meaning and therefore should not be construed as limiting the scope of protection of this invention.

[0053] Furthermore, the technical features involved in the different embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.

[0054] In a first aspect, the present invention provides a high-pressure fluidized bed reactor for producing aromatics from syngas. Figure 1 A schematic diagram of the high-pressure fluidized bed reactor for syngas-to-aromatics provided in an embodiment of the present invention is shown, as follows: Figure 1 As shown, the fluidized bed reactor 1 has an air distribution plate 101, an internal component 102, and a built-in cyclone separator 103 arranged sequentially along the gas flow direction in its chamber. The air distribution plate 101 is a metal air distribution plate with nozzle-type channels 1011 distributed thereon. The total area of ​​the nozzle-type channels 1011 accounts for 3% to 10% of the area of ​​the air distribution plate. The mesh size of the air distribution plate 101, except for the nozzle-type channels 1011, is 200 to 500 mesh.

[0055] Figure 2 A partial schematic diagram of the high-pressure fluidized bed reactor for producing aromatics from syngas provided in an embodiment of the present invention is shown, as follows: Figure 2 As shown, the internal component 102 is composed of aerodynamic components 1021 and guide plates 1022 arranged at intervals, and the total number of layers is an odd number. The first layer of the internal component 102 on the side closest to the air distribution plate 101 is the aerodynamic component.

[0056] Figure 1 , Figure 2 The high-pressure fluidized bed reactor shown has an air distribution plate 101 with nozzle-type channels 1011 above the inlet of the reactant gas. This allows the reactant gas, which already has a certain pressure (3-7 MPa), to enter the reactor and form multiple impinging airflows during its ascent. These impinges impact the catalyst particles packed inside the reactor, making fluidization easier. Combined with the inclusion of 200-500 mesh microchannels, uniform gas intake can be achieved.

[0057] Furthermore, an internal component 102, consisting of spaced-apart baffles 1021 and guide plates 1022, is disposed above the air distribution plate 101. The gas-solid mixture formed by the fluidization of the catalyst and feed gas is first altered by the baffles 1021, changing the flow path and velocity distribution of the feed gas and catalyst particles, creating strong turbulent dynamics. This reduces the accumulation and aggregation of catalyst particles, effectively controlling the uniformity of the bed and the mass transfer effect. The guide plates 1022 and baffles 1021 are arranged at intervals to adjust the contact and mixing degree between the gas and solid phases, increase the residence time of catalyst particles, change the gas-solid flow distribution, and improve the mass transfer effect, thereby increasing the reaction efficiency of syngas to aromatics production.

[0058] The flow-dispersing element provided by this invention can be in the shape of a water droplet and / or a cylinder; the guide plate can be in the shape of a rhombus or a triangle. The flow-dispersing element has a cooling liquid channel inside for circulating cooling water or coolant, which allows the flow-dispersing element to enhance heat and mass transfer inside the high-pressure fluidized bed reactor while effectively removing excess heat from the reaction zone, ensuring a uniform temperature distribution in the reaction zone during the reaction process.

[0059] Figure 3 The diagram shows a schematic representation of the built-in cyclone separator provided in an embodiment of the present invention, where a is a front view and b is a top view. Figure 3 As shown, the gas-solid inlet channel of the built-in cyclone separator 103 is equipped with an inverted triangular inertial baffle 1031, which is arranged in two staggered rows for preliminary separation of larger solid particles. The gas outlet of the built-in cyclone separator 103 is equipped with a corrugated filter screen 1032 to further separate the catalyst fine powder, preventing the catalyst fine powder from reacting uncontrollably with the outlet circulating gas and gaseous products in the cyclone separator, thus avoiding changes in product distribution. At the same time, the corrugated filter screen 1032 can increase the gas flow rate through this area, shorten the gas residence time here, and avoid the occurrence of side reactions.

[0060] Secondly, the present invention provides a cyclic system for producing aromatics from syngas. Figure 4 A schematic diagram of the syngas-to-aromatics cycle system provided in an embodiment of the present invention is shown, as follows: Figure 4As shown, the system includes: a high-pressure fluidized bed reactor 1 as described in the first aspect above, and a fractionation tower 2, a liquid separator 3, a water washing tank 4, a circulating pressurization pump 5, a mixing tank 6, and a preheating furnace 7; wherein, the outlet of the high-pressure fluidized bed reactor 1 is connected to the inlet of the fractionation tower 2, and the fractionation tower 2 is used to fractionate the mixed gas 1 of aromatic products, by-products, and unreacted gases discharged from the outlet of the high-pressure fluidized bed reactor 1 to collect and obtain liquid aromatic products; the operating pressure of the fractionation tower 2 is 2 MPa to 6 MPa, and a liquid outlet is provided at the bottom of the fractionation tower 2, which is connected to a liquid collection tank 8, which is used to collect the liquid aromatic products accumulated at the bottom of the fractionation tower 2 and transport them to the refining unit. The gas outlet at the top of fractionation tower 2 is connected to the inlet of separator 3, which is used to further remove liquid components from the mixed gas 2 discharged from the gas outlet of fractionation tower 2. The gas outlet of separator 3 is connected to the inlet of water washing tank 4, which is used to remove impurities from the mixed gas 3 discharged from the gas outlet of separator 3. The outlet of water washing tank 4 is connected to the inlet of circulating pressurization pump 5, which is used to pressurize the mixed gas 4 discharged from the outlet of water washing tank 4. The outlet of circulating pressurization pump 5 is connected to the inlet of mixing tank 6, which is used to mix the mixed gas 4 discharged from the outlet of circulating pressurization pump 5 with the raw material synthesis gas. The outlet of mixing tank 6 is connected to the inlet of preheating furnace 7, which is used to heat the mixed gas 5 discharged from the outlet of mixing tank 6. The outlet of preheating furnace 7 is connected to the raw material gas inlet of high-pressure fluidized bed reactor 1. High-pressure fluidized bed reactor 1 uses the mixed gas 5 discharged from the outlet of preheating furnace 7 as the reaction raw material and obtains aromatic products under the action of a bifunctional catalyst.

[0061] The present invention provides a syngas-to-aromatics recycling system and method. This system, based on a high-pressure fluidized bed reactor, incorporates a fractionation tower, a separator, a washing tank, a circulating pressurization pump, a mixing tank, and a preheating furnace to recycle unreacted syngas, further improving syngas conversion rate and aromatics yield. The syngas-to-aromatics recycling system provided by this invention has a simple equipment structure and a short process flow, showing great potential for application in important chemical technologies such as one-step aromatics production.

[0062] Thirdly, the present invention provides a method for producing aromatics from syngas, which is applicable to the syngas-to-aromatics cycle system described in the second aspect above. Figure 5 A flowchart of the method for producing aromatics from syngas provided in an embodiment of the present invention is shown, as follows: Figure 5 The methods shown include:

[0063] S1. Load a bimetallic catalyst into a high-pressure fluidized bed reactor and pass syngas into the high-pressure fluidized bed reactor. Under the action of the bifunctional catalyst, the syngas yields aromatic products.

[0064] S2. The mixed gas 1 containing aromatic products is discharged from the outlet of the high-pressure fluidized bed reactor and introduced through the inlet of the fractionation tower to fractionate the mixed gas and obtain liquid aromatic products.

[0065] S3. The remaining mixed gas 2 after fractionation is discharged from the gas outlet at the top of the fractionation tower and introduced through the inlet of the liquid separator to further remove the liquid components in the mixed gas 2.

[0066] S4. The remaining mixed gas 3 after removing the liquid components is discharged from the gas outlet of the separator and introduced through the inlet of the water washing tank to remove impurities in the mixed gas 3.

[0067] S5. The remaining mixed gas 4 after removing impurities is discharged from the outlet of the water washing tank and introduced through the inlet of the circulating pressurization pump to pressurize the mixed gas 4.

[0068] S6. The pressurized mixed gas 4 is discharged from the outlet of the circulating pressurization pump and introduced through the inlet of the mixing tank to mix the raw material synthesis gas and mixed gas 4 to obtain mixed gas 5.

[0069] S7. Discharge the mixed gas 5 from the outlet of the mixing tank and introduce it through the inlet of the preheating furnace to heat the mixed gas 5;

[0070] S8. The heated mixed gas 5 is discharged from the outlet of the preheating furnace and introduced into the feed gas inlet of the high-pressure fluidized bed reactor. Under the action of the bifunctional catalyst, aromatic products are obtained.

[0071] In some embodiments, the temperature inside the high-pressure fluidized bed reactor is 250–550°C, and the pressure is 2 MPa–6 MPa; the pressure during operation of the fractionation tower is 2 MPa–6 MPa.

[0072] In some embodiments, the bifunctional catalyst has a particle size of 50–150 μm and the loading of the bifunctional catalyst is 3–5 times the height-to-diameter ratio of the high-pressure fluidized bed reactor.

[0073] In some embodiments, the volume ratio of CO to H2 in the synthesis gas is 1:1 to 1:1; the circulation ratio of the mixed gas 4 is 2.5 to 6.

[0074] To enable those skilled in the art to more clearly understand the present invention, the following embodiments will be used to provide a detailed description of a high-pressure fluidized bed reactor, circulation system, and method for producing aromatics from syngas according to the present invention.

[0075] Example 1

[0076] The high-pressure fluidized bed reactor 1, fractionation tower 2, separating tank 3, washing tank 4, circulating pressurization pump 5, mixing tank 6, preheating furnace 7, and receiving tank 8 are arranged according to the attached... Figure 4The schematic diagram shown is connected to form a fully functional system. In the high-pressure fluidized bed reactor 1 for syngas to aromatics described in this invention, 30t of bifunctional catalyst is loaded. The bed height in the reactor is 5m. The required syngas composition is H2 / CO = 1, and the syngas flow rate is 5250 Nm³. 3 / hr, the circulation ratio of the gas supply system is 4, the temperature of the high-pressure fluidized bed reactor during operation is 350℃, the reaction pressure is 4MPa, after a long period of stable operation, the selectivity of aromatics is 85%, and the conversion rate of CO is 99.5%.

[0077] Example 2

[0078] The high-pressure fluidized bed reactor 1, fractionation tower 2, separating tank 3, washing tank 4, circulating pressurization pump 5, mixing tank 6, preheating furnace 7, and receiving tank 8 are arranged according to the attached... Figure 4 The schematic diagram shown is connected to form a fully functional system. In the high-pressure fluidized bed reactor 1 for syngas to aromatics described in this invention, a bifunctional catalyst of 30t is loaded. The bed height in the reactor is 7m. The required syngas composition is H2 / CO = 1.1, and the syngas supply is set to a CO flow rate of 4300 Nm³. 3 / hr, the circulation ratio of the gas supply system is 4, the temperature of the high-pressure fluidized bed reactor during operation is 300℃, the reaction pressure is 3.5MPa, after a long period of stable operation, the selectivity of aromatics is 80%, and the conversion rate of CO is 98%.

[0079] Example 3

[0080] The high-pressure fluidized bed reactor 1, fractionation tower 2, separating tank 3, washing tank 4, circulating pressurization pump 5, mixing tank 6, preheating furnace 7, and receiving tank 8 are arranged according to the attached... Figure 4 The schematic diagram shown is connected to form a fully functional system. In the high-pressure fluidized bed reactor 1 for syngas to aromatics described in this invention, a bifunctional catalyst of 45t is loaded. The bed height in the reactor is 7m. The required syngas composition for the reaction is H2 / CO = 1, and the syngas supply is set to a CO flow rate of 5500 Nm³. 3 / hr, the circulation ratio of the gas supply system is 4, the temperature of the high-pressure fluidized bed reactor during operation is 325℃, the reaction pressure is 4.5MPa, after a long period of stable operation, the selectivity of aromatics is 88%, and the conversion rate of CO is 100%.

[0081] Example 4

[0082] The high-pressure fluidized bed reactor 1, fractionation tower 2, separating tank 3, washing tank 4, circulating pressurization pump 5, mixing tank 6, preheating furnace 7, and receiving tank 8 are arranged according to the attached... Figure 4The schematic diagram shown is connected to form a fully functional system. The high-pressure fluidized bed reactor 1 for syngas to aromatics described in this invention is loaded with a bifunctional catalyst of 25t. The bed height in the reactor is 5m. The required syngas composition is H2 / CO = 1, and the syngas supply is set to a CO flow rate of 4000 Nm³. 3 / hr, the circulation ratio of the gas supply system is 5, the temperature of the high-pressure fluidized bed reactor is 300℃ and the reaction pressure is 4MPa during operation. After a long period of stable operation, the selectivity of aromatics is 87% and the conversion rate of CO is 100%.

[0083] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. In addition, those skilled in the art can combine and integrate the different embodiments or examples described in this specification.

[0084] For the sake of simplicity, the method embodiments are described as a series of actions. However, those skilled in the art should understand that the present invention is not limited to the described order of actions, as some steps can be performed in other orders or simultaneously according to the present invention. Furthermore, those skilled in the art should also understand that the embodiments described in the specification are preferred embodiments, and the actions and components involved are not necessarily essential to the present invention.

[0085] The above provides a detailed description of a high-pressure fluidized bed reactor, circulation system, and method for producing aromatics from syngas, as provided by the present invention. Specific examples have been used to illustrate the principles and implementation methods of the present invention. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of the present invention. At the same time, for those skilled in the art, there will be changes in the specific implementation methods and application scope based on the ideas of the present invention. Therefore, the content of this specification should not be construed as a limitation of the present invention.

Claims

1. A cyclic system for producing aromatics from syngas, characterized in that, include: High-pressure fluidized bed reactor, fractionation tower, separator, washing tank, circulating pressurization pump, mixing tank, and preheating furnace; among which, The high-pressure fluidized bed reactor is provided with an air distribution plate, internal components and a built-in cyclone separator arranged sequentially along the gas flow direction in the chamber. The air distribution plate is a metal air distribution plate with nozzle-type channels distributed thereon, and the total area of ​​the nozzle-type channels accounts for 3% to 10% of the area of ​​the air distribution plate; the mesh size of the air distribution plate in other areas except for the nozzle-type channels is 200 to 500 mesh. The internal components are composed of spaced-apart spoilers and guide vanes, and the total number of layers is an odd number. The first layer of the internal components on the side closest to the air distribution plate is the spoiler. The gas-solid inlet channel of the built-in cyclone separator is equipped with an inverted triangular inertial baffle, which is arranged in two staggered rows for the initial separation of larger solid particles. The outlet of the high-pressure fluidized bed reactor is connected to the inlet of the fractionation tower, which is used to fractionate the mixed gas 1 containing aromatic products discharged from the outlet of the high-pressure fluidized bed reactor to obtain liquid aromatic products. The gas outlet at the top of the fractionation tower is connected to the inlet of the liquid separator, which is used to further remove the liquid component from the mixed gas 2 discharged from the gas outlet of the fractionation tower. The gas outlet of the separator is connected to the inlet of the water washing tank, and the water washing tank is used to remove impurities from the mixed gas 3 discharged from the gas outlet of the separator. The outlet of the washing tank is connected to the inlet of the circulating pressurizing pump, which is used to pressurize the mixed gas 4 discharged from the outlet of the washing tank. The outlet of the circulating pressurizing pump is connected to the inlet of the mixing tank, and the mixing tank is used to mix the mixed gas 4 discharged from the outlet of the circulating pressurizing pump with the raw material synthesis gas; The outlet of the mixing tank is connected to the inlet of the preheating furnace, and the preheating furnace is used to heat the mixed gas 5 discharged from the outlet of the mixing tank; The outlet of the preheating furnace is connected to the feed gas inlet of the high-pressure fluidized bed reactor. The high-pressure fluidized bed reactor uses the mixed gas 5 discharged from the outlet of the preheating furnace as the reaction feedstock and obtains aromatic products under the action of a bifunctional catalyst.

2. The syngas-to-aromatics recycling system according to claim 1, characterized in that, The turbulence-disrupting element is in the shape of a water droplet and / or a cylinder; the guide plate is in the shape of a rhombus or a triangle.

3. The syngas-to-aromatics recycling system according to claim 1, characterized in that, The aerodynamic component has a coolant channel inside.

4. The syngas-to-aromatics recycling system according to claim 1, characterized in that, The gas outlet of the built-in cyclone separator is equipped with a corrugated filter screen for further separation of catalyst fine powder.

5. The syngas-to-aromatics recycling system according to claim 1, characterized in that, The fractionation tower is provided with a liquid outlet at the bottom, which is connected to a liquid collection tank. The liquid collection tank is used to collect the liquid aromatic products that accumulate at the bottom of the fractionation tower.

6. A method for producing aromatics from syngas, characterized in that, The method is applicable to the syngas-to-aromatics cycle system described in claim 1 or 5 above, and the method includes: S1. Load a bimetallic catalyst into a high-pressure fluidized bed reactor and introduce syngas into the high-pressure fluidized bed reactor. Under the action of the bifunctional catalyst, the syngas yields aromatic products. S2. The mixed gas 1 containing aromatic products is discharged from the outlet of the high-pressure fluidized bed reactor and introduced through the inlet of the fractionation tower to fractionate the mixed gas and obtain liquid aromatic products. S3. The remaining mixed gas 2 after fractionation is discharged from the gas outlet at the top of the fractionation tower and introduced through the inlet of the liquid separator to further remove the liquid components in the mixed gas 2. S4. The remaining mixed gas 3 after removing the liquid components is discharged from the gas outlet of the separator and introduced through the inlet of the water washing tank to remove impurities in the mixed gas 3. S5. The remaining mixed gas 4 after removing impurities is discharged from the outlet of the water washing tank and introduced through the inlet of the circulating pressurization pump to pressurize the mixed gas 4. S6. The pressurized mixed gas 4 is discharged from the outlet of the circulating pressurization pump and introduced through the inlet of the mixing tank to mix the raw material synthesis gas and mixed gas 4 to obtain mixed gas 5. S7. Discharge the mixed gas 5 from the outlet of the mixing tank and introduce it through the inlet of the preheating furnace to heat the mixed gas 5; S8. The heated mixed gas 5 is discharged from the outlet of the preheating furnace and introduced into the feed gas inlet of the high-pressure fluidized bed reactor. Under the action of the bifunctional catalyst, aromatic products are obtained.

7. The method for producing aromatics from syngas according to claim 6, characterized in that, The temperature inside the high-pressure fluidized bed reactor is 250~550 ℃, and the pressure is 2 MPa~6 MPa; The distillation tower operates at a pressure of 2 MPa to 6 MPa.

8. The method for producing aromatics from syngas according to claim 6, characterized in that, The bifunctional catalyst has a particle size of 50-150 μm, and the loading of the bifunctional catalyst is 3-5 times the height-to-diameter ratio of the high-pressure fluidized bed reactor.

9. The method for producing aromatics from syngas according to claim 6, characterized in that, In the synthesis gas, the volume ratio of CO to H2 is 1:1 to 1:1; The circulation ratio of the mixed gas 4 is 2.5 to 6.

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