Reaction system for preparing high alcohols from Fischer-Tropsch long-chain olefins

Abstract

The invention relates to a reaction system for preparing high alcohols from Fischer-Tropsch long-chain olefins, the reaction system comprises a hydroformylation reactor, a rotary falling film evaporator, a hydrogenation reactor, a gas-liquid separator and a rectification device, the bottom of the hydroformylation reactor is provided with a gas inlet pipeline, and is uniformly provided with a plurality of gas distributors; the synthesis gas is uniformly diffused into the hydroformylation reactor from the gas distributor; the rotary falling film evaporator is communicated with the hydroformylation reactor; a communicating pipeline is arranged at the top of the rotary falling-film evaporator and is communicated with the hydrogenation reactor; the gas-liquid separator is communicated with the hydrogenation reactor; and the rectification device is communicated with the gas-liquid separator. According to the reaction system for preparing high alcohols from Fischer-Tropsch long-chain olefins, the plurality of gas distributors are uniformly arranged at the bottom of the hydroformylation reactor, so that synthesis gas can be uniformly dispersed in the reactor and fully contacted with reaction raw materials, the mass transfer efficiency between gas and liquid is improved, and the conversion rate of Fischer-Tropsch long-chain olefins is improved.

Description

Technical Field

[0001] The present disclosure relates to the field of chemical technology, and more specifically, to a reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins. Background Art

[0002] As an important chemical raw material, high carbon alcohols are widely used in many industrial fields, such as daily chemical products, textile auxiliaries and the manufacture of various synthetic materials. In the process of preparing high carbon alcohols from olefins, hydroformylation reaction is a crucial step, which first converts olefins into corresponding aldehydes, and then the aldehydes are further converted into high carbon alcohols through hydrogenation reaction. This series of reactions is crucial for the production of lubricating base oils, surfactants, plasticizers and other fine chemicals. However, existing hydroformylation reactors often face the problem of low mass transfer efficiency, resulting in low conversion rate of olefins in the reactor, reducing reaction efficiency, reducing the yield of the final product, and increasing production costs. Summary of the invention

[0003] In view of this, the embodiments of the present disclosure provide a reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins to solve the technical defects existing in the prior art.

[0004] To achieve the above objectives, the present disclosure adopts the following technical solutions: The present disclosure provides a reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins, comprising: A hydroformylation reactor, wherein an air inlet pipeline is arranged at the bottom of the hydroformylation reactor, and a plurality of gas distributors are evenly arranged, wherein the gas distributor is in communication with the air inlet pipeline, and the synthesis gas enters the gas distributor from the air inlet pipeline and is evenly diffused from the gas distributor into the hydroformylation reactor, wherein the hydroformylation reactor is used for reacting the Fischer-Tropsch long-chain olefins with the synthesis gas to generate a first liquid phase; A rotary falling film evaporator, the rotary falling film evaporator is connected to the hydroformylation reactor and is used to separate the first liquid phase into a second liquid phase and a third liquid phase; A hydrogenation reactor, wherein a connecting pipe is disposed on the top of the rotary falling film evaporator, the connecting pipe is connected to the hydrogenation reactor, and the hydrogenation reactor is configured to cause the second liquid phase to undergo a hydrogenation reaction to generate a fourth liquid phase; a gas-liquid separator, the gas-liquid separator being in communication with the hydrogenation reactor, the gas-liquid separator being configured to separate the fourth liquid phase from hydrogen in the fourth liquid phase; A distillation device is connected to the gas-liquid separator, and is used for distilling the fourth liquid phase into high-carbon alcohols and heavy oil fractions.

[0005] In one embodiment of the present disclosure, the gas distributor includes a gas distributor body and a distributor interface, and the gas distributor body is connected to the gas inlet pipeline through the distributor interface.

[0006] In one embodiment of the present disclosure, the air inlet pipe includes at least a vertical portion and a horizontal portion, one end of the vertical portion is connected to the outside of the hydroformylation reactor, and the other end is connected to the horizontal portion, the horizontal portion is horizontally arranged at the bottom of the hydroformylation reactor, and the gas distributors are all connected to the horizontal portion.

[0007] In one embodiment of the present disclosure, the vertical portion includes at least two vertical segments and one bending segment, and the bending segment is arranged between the two vertical segments.

[0008] In one embodiment of the present disclosure, the gas distributors are evenly distributed in the circumferential direction.

[0009] In one embodiment of the present disclosure, the gas distributor is circumferentially arranged at the bottom of the hydroformylation reactor, and the distance between adjacent gas distributors is equal to the radius of the gas diffusion range of each gas distributor.

[0010] In one embodiment of the present disclosure, a temperature measuring port is further provided on the top of the hydroformylation reactor, and a temperature measuring tube is further provided inside the reactor, and the temperature measuring tube passes into the interior of the hydroformylation reactor through the temperature measuring port.

[0011] In one embodiment of the present disclosure, the hydroformylation reactor is a high-pressure reactor, and the temperature inside the hydroformylation reactor is 80° C. to 240° C., and the pressure is 2 MPa to 8 MPa.

[0012] In one embodiment of the present disclosure, the pore size of the gas distributor is 1 μm to 100 μm.

[0013] In one embodiment of the present disclosure, the distillation device includes a light-removing tower, a refining tower and a heavy-removing tower, the light-removing tower is connected to the gas-liquid separator, the refining tower is connected to the light-removing tower, and the heavy-removing tower is connected to the refining tower.

[0014] The reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins provided in the present invention has multiple gas distributors evenly arranged at the bottom of the hydroformylation reactor, so that the synthesis gas can be evenly dispersed in the reactor and fully contact with the reaction raw materials, thereby improving the mass transfer efficiency between gas and liquid and improving the conversion rate of Fischer-Tropsch long-chain olefins.

[0015] Other features and advantages of the present disclosure will become apparent from the following detailed description of exemplary embodiments of the present disclosure with reference to the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 It is a schematic structural diagram of a reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins provided in one embodiment of the present disclosure; Figure 2 is a schematic structural diagram of a hydroformylation reactor provided in one embodiment of the present disclosure; Figure 3 is a schematic diagram of the specific structure of a gas distributor provided in one embodiment of the present disclosure; Figure 4 is a distribution diagram of a gas distributor provided by an embodiment of the present disclosure; Figure 5 It is a distribution diagram of a gas distributor provided in another embodiment of the present disclosure.

[0017] 1-hydroformylation reactor; 11-air inlet pipe; 111-vertical part; 112-horizontal part; 12-gas distributor; 121-gas distributor body; 122-distributor interface; 13-temperature measuring port; 14-temperature measuring tube; 15-feeding port; 16-gas outlet; 17-pressure measuring port; 2-rotary falling film evaporator; 3-hydrogenation reactor; 4-gas-liquid separator; 5-distillation device; 51-lightness removal tower; 52-refining tower; 53-heavyness removal tower. DETAILED DESCRIPTION

[0018] Various exemplary embodiments of the present disclosure will now be described in detail with reference to the accompanying drawings. It should be noted that the relative arrangement of components and steps, numerical expressions and numerical values ​​set forth in these embodiments do not limit the scope of the present disclosure unless otherwise specifically stated.

[0019] The following description of at least one exemplary embodiment is merely illustrative in nature and is in no way intended to limit the present disclosure, its application, or uses.

[0020] Technologies, methods, and equipment known to ordinary technicians in the relevant art may not be discussed in detail, but where appropriate, the technologies, methods, and equipment should be considered as part of the specification.

[0021] It should be noted that like reference numerals and letters refer to similar items in the following figures, and therefore, once an item is defined in one figure, it need not be further discussed in subsequent figures.

[0022] The specific embodiments of the present disclosure are described below in conjunction with the accompanying drawings.

[0023] In this document, “upper”, “lower”, “front”, “back”, “left”, “right”, etc. are only used to indicate the relative position relationship between related parts, rather than to limit the absolute positions of these related parts.

[0024] In this article, "first", "second", etc. are only used to distinguish each other, and do not indicate the importance and order, or the premise of each other's existence.

[0025] In this document, “equal”, “same”, etc. are not strictly limited in a mathematical and / or geometric sense, but also include errors that can be understood by those skilled in the art and are allowed in manufacturing or use.

[0026] The present invention provides a reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins, comprising a hydroformylation reactor, a rotary falling film evaporator, a hydrogenation reactor, a gas-liquid separator and a distillation device. Among them, an air inlet pipe is arranged at the bottom of the hydroformylation reactor, and a plurality of gas distributors are evenly arranged, the gas distributor is connected to the air inlet pipe, the synthesis gas enters the gas distributor from the air inlet pipe, and is evenly diffused from the gas distributor into the hydroformylation reactor, the hydroformylation reactor is used for the reaction of Fischer-Tropsch long-chain olefins with the synthesis gas to generate a first liquid phase; the rotary falling film evaporator is connected to the hydroformylation reactor, and is used to separate the first liquid phase into a second liquid phase and a third liquid phase; a connecting pipe is arranged at the top of the rotary falling film evaporator, and the connecting pipe is connected to the hydrogenation reactor, and the hydrogenation reactor is configured to hydrogenate the second liquid phase to generate a fourth liquid phase; the gas-liquid separator is connected to the hydrogenation reactor, and the gas-liquid separator is configured to separate the fourth liquid phase and the hydrogen in the fourth liquid phase; the distillation device is connected to the gas-liquid separator, and the distillation device is used to distill the fourth liquid phase into high-carbon alcohols and heavy oil fractions.

[0027] The present invention provides a reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins. By evenly arranging a plurality of gas distributors at the bottom of a hydroformylation reactor, the synthesis gas can be evenly dispersed in the reactor and fully contact with the reaction raw materials, thereby improving the mass transfer efficiency between gas and liquid and improving the conversion rate of the Fischer-Tropsch long-chain olefins.

[0028] For ease of understanding, refer to Figures 1 to 5 , the specific structure and working principle of the reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins disclosed in the present invention are explained in detail with reference to an embodiment.

[0029] like Figure 1 As shown, the reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins in this embodiment includes a hydroformylation reactor 1, a rotary falling film evaporator 2, a hydrogenation reactor 3, a gas-liquid separator 4 and a distillation device 5.

[0030] An air inlet pipe 11 is provided at the bottom of the hydroformylation reactor 1, and a plurality of gas distributors 12 are evenly provided. The gas distributor 12 is connected to the air inlet pipe 11. The synthesis gas enters the gas distributor 12 from the air inlet pipe 11 and is evenly diffused from the gas distributor 12 into the hydroformylation reactor 1. The hydroformylation reactor 1 is used for the reaction of Fischer-Tropsch long-chain olefins with the synthesis gas to generate a first liquid phase.

[0031] Specifically, the air inlet pipe 11 is a passage for the synthesis gas (usually containing carbon monoxide and hydrogen) to enter the hydroformylation reactor 1. A plurality of gas distributors 12 are evenly arranged at the bottom of the hydroformylation reactor 1. Each gas distributor 12 is connected to the air inlet pipe 11. A plurality of small holes or slits are arranged on the gas distributor 12. The synthesis gas enters the plurality of gas distributors 12 through the air inlet pipe 11 and is evenly diffused into the hydroformylation reactor 1 from the small holes or slits of the plurality of gas distributors 12. The gas distributors 12 evenly arranged at the bottom of the hydroformylation reactor 1 can ensure that the synthesis gas is fully in contact with the Fischer-Tropsch long-chain olefins, improve the gas-liquid mass transfer efficiency, and thus improve the reaction efficiency. In the hydroformylation reactor 1, the Fischer-Tropsch long-chain olefins react with the synthesis gas under the action of the catalyst to generate a first liquid phase, which includes the generated aldehyde substances, the catalyst solution, and the reaction raw materials that do not participate in the reaction. In this embodiment, the catalyst in the catalyst solution can be a carbonyl cobalt compound, a rhodium compound and / or a complex, such as octacarbonyl dicobalt, cobalt diisooctanoate, rhodium acetylacetonate, etc.; the catalyst ligand can be selected from BISBI, triphenylphosphine, 4,5-bis(diphenylphosphine)-9,9-dimethyloxanthene and other commonly used phosphine ligands; the catalyst solvent can be selected from one or more of ethanol, cyclohexane, toluene or xylene, etc., without any limitation. In this embodiment, the Fischer-Tropsch long-chain olefin is an olefin with a carbon number greater than 10. Since the olefin has a large molecular weight and diffuses slowly as a reaction raw material, a plurality of gas distributors 12 are evenly arranged at the bottom of the hydroformylation reactor 1, which can improve the mass transfer efficiency between the Fischer-Tropsch long-chain olefin and the synthesis gas, thereby improving the conversion rate of the Fischer-Tropsch long-chain olefin.

[0032] The rotary falling film evaporator 2 is connected to the hydroformylation reactor 1 and is used to separate the first liquid phase into a second liquid phase and a third liquid phase.

[0033] Specifically, the rotary falling film evaporator 2 is connected to the hydroformylation reactor 1 and is used to separate the first liquid phase generated by the hydroformylation reaction. After the first liquid phase enters the rotary falling film evaporator 2, the liquid forms a thin falling film through the rotating structure of the rotary falling film evaporator 2 and flows along the heating surface of the evaporator. During this process, the pressure of the rotary falling film evaporator 2 is 0.15MPa and the temperature is 285°C. Due to the high thermal efficiency provided by the heating surface, the volatile components in the liquid evaporate rapidly, while the heavier non-volatile components remain in the evaporator as the third liquid phase.

[0034] The design of the rotary falling film evaporator 2 enables the liquid film to be evenly distributed and quickly renewed, thereby improving the heat transfer efficiency and evaporation rate, while reducing the possibility of scaling. In this way, the first liquid phase is effectively separated into two parts: one part is steam containing a high concentration of volatile components, which forms a second liquid phase after condensation, and the second liquid phase contains aldehyde substances; the other part is a non-volatile component, that is, a third liquid phase, which contains a catalyst solution, and the catalyst solution can be transported to the hydroformylation reactor 1 again via the rotary falling film evaporator 2 for recycling. Through such a separation process, the reaction product can be effectively separated from other components, which facilitates further refining and purification, and ultimately obtains high-quality target chemicals.

[0035] A connecting pipe is provided on the top of the rotary falling film evaporator 2, and the connecting pipe is connected to the hydrogenation reactor 3. The hydrogenation reactor 3 is configured to cause the second liquid phase to undergo a hydrogenation reaction to generate a fourth liquid phase.

[0036] Specifically, a connecting pipe is provided at the top of the rotary falling film evaporator 2, and the pipe is connected to the hydrogenation reactor 3. In the hydrogenation reactor 3, the second liquid phase reacts with hydrogen under the action of a catalyst. The presence of the catalyst accelerates the chemical bonding between hydrogen molecules and various components in the second liquid phase, prompting these components to undergo a hydrogenation reaction. The hydrogenation reaction can be used to reduce unsaturated bonds (such as double bonds or triple bonds), or to convert certain functional groups (such as nitro or carbonyl groups) into more stable structures, thereby generating new compounds.

[0037] After the hydrogenation reaction, the generated product is a fourth liquid phase, and the fourth liquid phase contains alcohol substances generated by the hydrogenation reaction. In this embodiment, the hydrogenation reactor 3 uses a fixed bed hydrogenation reactor 3, and the conditions in the hydrogenation reactor 3 (such as temperature, pressure and catalyst type) can be adjusted according to the characteristics of the desired product to optimize the selectivity and yield of the reaction. In this embodiment, the reaction temperature in the hydrogenation reactor 3 is 80°C to 199°C, and the reaction pressure is 3MPa to 5MPa. Through the continuous operation of the rotary falling film evaporator 2 and the hydrogenation reactor 3, effective separation and conversion of complex mixtures can be achieved, and the desired target chemicals are finally obtained.

[0038] The gas-liquid separator 4 is connected to the hydrogenation reactor 3 , and is configured to separate the fourth liquid phase from the hydrogen in the fourth liquid phase.

[0039] Specifically, in the hydrogenation reactor 3, the second liquid phase and hydrogen react with each other under the action of a catalyst to generate a new compound, namely the fourth liquid phase. In this process, incompletely reacted hydrogen and other volatile by-products will exist together with the liquid product. The fourth liquid phase coming out of the hydrogenation reactor 3 enters the gas-liquid separator 4, and the fourth liquid phase is deposited at the bottom of the separator due to gravity, while the lighter gas phase (mainly the remaining hydrogen and other volatile components) can be discharged through the outlet at the top and re-enter the hydrogenation reactor 3 for recycling.

[0040] This separation process helps to recover unused hydrogen for recycling, improving the overall efficiency and economy of the reaction. At the same time, the separated fourth liquid phase can be further sent to subsequent processing units to achieve higher purity requirements.

[0041] The distillation device 5 is connected to the gas-liquid separator 4, and the distillation device 5 is used for distilling the fourth liquid phase into high-carbon alcohols and heavy oil fractions.

[0042] Specifically, the distillation device 5 is used to distill the fourth liquid phase into high-carbon alcohols and heavy oil fractions. In the distillation device 5, the components in the mixture are separated by multiple partial evaporations and condensations. At the top of the distillation device 5, light components with low boiling points, i.e., high-carbon alcohols, are collected; and at the bottom of the distillation device 5, heavy oil fractions with high boiling points are collected.

[0043] The reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins increases the contact area between Fischer-Tropsch long-chain olefins and synthesis gas through a multi-stage separation device and a uniform arrangement of the gas distributor 12 in the hydroformylation reactor 1, thereby increasing the conversion rate of the Fischer-Tropsch long-chain olefins and reducing production costs.

[0044] like Figures 2 to 3 As shown, in one embodiment of the present disclosure, the gas distributor 12 includes a gas distributor body 121 and a distributor interface 122 , and the gas distributor body 121 is connected to the gas inlet pipe 11 through the distributor interface 122 .

[0045] Specifically, the gas distributor 12 is one of the key components in the hydroformylation reactor 1, and includes a gas distributor body 121 and a distributor interface 122. The gas distributor body 121 is a component that actually performs the gas distribution function, and is usually configured to have a structure with multiple tiny holes or slits to ensure that the gas can be evenly dispersed into the liquid in the reactor. The distributor interface 122 is a part that connects the gas distributor body 121 and the air inlet pipe 11, and is used to introduce the synthesis gas transported from the air inlet pipe 11 into the gas distributor body 121.

[0046] Through the connection between the distributor interface 122 and the gas inlet pipe 11, the synthesis gas can stably enter the gas distributor body 121 and be evenly released into the liquid in the reactor through the holes or slits on the body, which helps to ensure the uniform distribution of the reactants in the reactor, thereby improving the reaction efficiency. Uniform gas distribution can also avoid excessively high or low gas concentrations in local areas, and prevent side reactions or product quality degradation caused by inconsistent reaction conditions.

[0047] In one embodiment of the present disclosure, the air inlet pipe 11 includes at least a vertical portion 111 and a horizontal portion 112, one end of the vertical portion 111 is connected to the outside of the hydroformylation reactor 1, and the other end is connected to the horizontal portion 112, the horizontal portion 112 is horizontally arranged at the bottom of the hydroformylation reactor 1, and the gas distributors 12 are all connected to the horizontal portion 112.

[0048] Specifically, one end of the vertical portion 111 is connected to the outside of the hydroformylation reactor 1, that is, the synthesis gas is transported from the external environment to the inside of the reactor. The design of the vertical portion 111 is generally to facilitate the gas to enter the reactor vertically from the top, which can reduce the resistance when the gas enters and help the gas to be better distributed in the entire reactor space. The other end of the vertical portion 111 is connected to the horizontal portion 112, which is arranged at the bottom of the hydroformylation reactor 1. The arrangement of the horizontal portion 112 allows the synthesis gas to flow horizontally at the bottom of the reactor and be evenly released into the reaction medium through a plurality of gas distributors 12 connected thereto. This layout helps to ensure that the gas can be evenly distributed at the bottom of the reactor and further diffused into the entire hydroformylation reactor 1.

[0049] In one embodiment of the present disclosure, the vertical portion 111 includes at least two vertical segments and one bending segment, and the bending segment is disposed between the two vertical segments.

[0050] The vertical portion 111 of the air inlet pipe 11 is configured to include at least two vertical sections and one bending section. Such a structure can more reasonably guide the gas into the hydroformylation reactor 1 and help reduce the resistance and turbulence in the gas flow. The first vertical section starts from the outside of the hydroformylation reactor 1 and extends upward. The main function of this vertical section is to introduce synthesis gas from the outside and guide it to the next section. The bending section is located between the two vertical sections and plays the role of connecting the upper and lower vertical sections. The design of the bending section can be L-shaped, U-shaped or other shapes. The specific shape depends on actual needs and spatial layout, and no limitation is made here. The design of the bending section helps to smoothly change the flow direction of the gas, reduce the resistance when the gas flows, and help to better control the speed and direction of the gas entering the hydroformylation reactor 1. The second vertical section extends upward from the bending section until it is connected to the horizontal section 112. The design of the second vertical section helps to further guide the gas and make it smoothly transition to the horizontal section 112.

[0051] Through the design of two vertical sections and one bending section, the gas can have a relatively uniform distribution trend before entering the horizontal portion 112, which is helpful for the subsequent operation of the gas distributor 12. And the angle and position of the bending section can be flexibly adjusted according to the actual spatial layout, so that the pipeline can adapt to different installation environments.

[0052] In one embodiment of the present disclosure, the gas distributors 12 are evenly distributed in the circumferential direction.

[0053] The uniform distribution design of the gas distributor 12 in the circumferential direction is to ensure that the synthesis gas can be evenly distributed inside the hydroformylation reactor 1, thereby improving the uniformity and efficiency of the reaction. Specifically, at the bottom of the hydroformylation reactor 1, the gas distributors 12 are evenly arranged at certain intervals. Such a layout ensures that the gas entering the reactor from all directions can be evenly distributed throughout the bottom of the reactor, thereby avoiding the situation where the local gas concentration is too high or too low. By evenly distributing the gas distributors 12 in the circumferential direction, uniform release of gas can be achieved. Each gas distributor 12 will release the gas into the reaction medium in the form of fine bubbles, increasing the gas-liquid contact area, facilitating sufficient contact between the reactants, improving the reaction efficiency, and avoiding local supersaturation in the reaction medium, reducing the occurrence of side reactions, thereby improving the yield and selectivity of the target product.

[0054] In addition, by controlling the number and spacing of the gas distributors 12, the gas distribution inside the reactor can be optimized to ensure that the reaction conditions in each area are as consistent as possible, which helps maintain the stability and controllability of the entire reaction process.

[0055] like Figures 4 to 5As shown, in one embodiment of the present disclosure, the gas distributors 12 are circumferentially arranged at the bottom of the hydroformylation reactor 1 , and the distance between adjacent gas distributors 12 is equal to the radius of the gas diffusion range of each gas distributor 12 .

[0056] Specifically, Figures 4 to 5 As shown, taking the arrangement of 4 gas distributors 12 and 42 gas distributors 12 as an example, the gas distributors 12 are distributed in a ring shape around the bottom of the hydroformylation reactor 1. This layout enables the gas to be released evenly from all directions of the bottom of the reactor, thereby covering the entire bottom area of ​​the reactor. The distance between adjacent gas distributors 12 is set to be equal to the radius of the gas diffusion range of each gas distributor 12, so that the gas released by each gas distributor 12 can just cover the area around it, and the gas diffusion ranges of adjacent distributors are connected to each other, so as to achieve the goal of covering as much of the bottom of the hydroformylation reactor 1 as possible with as few gas distributors 12 as possible, ensuring the uniform distribution of the gas at the bottom of the entire reactor, avoiding the unevenness of the local gas concentration, reducing the reaction dead corner, and thus improving the uniformity and efficiency of the reaction.

[0057] like Figure 2 As shown, in one embodiment of the present disclosure, a temperature measuring port 13 is further provided on the top of the hydroformylation reactor 1 , and a temperature measuring tube 14 is further provided inside. The temperature measuring tube 14 passes into the hydroformylation reactor 1 through the temperature measuring port 13 .

[0058] Specifically, the temperature measuring port 13 is located at the top of the reactor and is used to insert the temperature measuring tube 14. The temperature measuring port 13 has good sealing during use to prevent any leakage or external substances from entering the reactor during the measurement process. The temperature measuring tube 14 is usually equipped with a temperature sensor or probe, and the temperature sensor can accurately contact the reaction medium to obtain real temperature data. The length and diameter of the temperature measuring tube 14 need to be set according to the actual size and measurement requirements of the hydroformylation reactor 1. Through the temperature measuring tube 14, the temperature change inside the reactor can be monitored in real time, which helps to maintain better reaction conditions, reduce the occurrence of side reactions, and improve the yield of the target product. In addition, the measured temperature data can be used to adjust the operating conditions of the reactor in time to keep the temperature inside the reactor within a constant range. In addition to controlling the reaction conditions, real-time temperature monitoring also helps to detect any abnormal conditions early, such as a sudden increase or decrease in temperature, which may be a sign of a runaway reaction or other problems. Timely detection of these problems can take measures to prevent accidents.

[0059] like Figure 2As shown, in one embodiment of the present disclosure, a feed port 15, an air outlet 16 and a pressure measuring port 17 are provided on the hydroformylation reactor 1, which can ensure that the hydroformylation reactor 1 can operate safely and efficiently, and facilitate the operator to add raw materials, discharge gases and monitor pressure. The feed port 15 is used to put necessary raw materials into the hydroformylation reactor 1, which include Fischer-Tropsch long-chain olefins, catalysts, etc. The feed port 15 is usually provided with a sealing cover or valve to prevent gas leakage when no feed is added. When adding feed, it is necessary to ensure the safety of the feeding process and avoid introducing air or other impurities to avoid affecting the reaction. The air outlet 16 is used to discharge the gas in the hydroformylation reactor 1, including unreacted synthesis gas, by-product gas and other volatile components. The pressure measuring port 17 is used to monitor the pressure inside the hydroformylation reactor 1. The pressure data inside the hydroformylation reactor 1 can be obtained in real time through the pressure measuring port 17, which is crucial for controlling the reaction conditions and ensuring the safe operation of the reactor. The pressure measuring port 17 is generally connected through a pressure gauge or a pressure sensor, which can convert the pressure signal into easy-to-read data. The pressure measuring port 17 also needs to have good sealing properties to prevent gas leakage.

[0060] In one embodiment of the present disclosure, the hydroformylation reactor 1 is a high-pressure reactor, and the temperature in the hydroformylation reactor 1 is 80° C. to 240° C., and the pressure is 2 MPa to 8 MPa.

[0061] The hydroformylation reactor 1 is a high-pressure reactor, and its operating conditions are usually carried out at a higher temperature and pressure to ensure that the reaction can be carried out efficiently. In the temperature range of 80°C to 240°C, in this embodiment, 160°C to 240°C is preferably used as the temperature range of the reaction. In this temperature range, the activity of the reactants is enhanced, the reaction rate is accelerated, and it is helpful to improve the selectivity and yield of the product. The choice of temperature needs to be determined according to the specific catalyst type, reactant characteristics and target product to achieve a better reaction effect. The pressure range is 2MPa to 8MPa. Under high pressure conditions, the solubility of the reactants can be increased, the gas-liquid contact area can be increased, and the reaction rate can be accelerated. In this embodiment, 4MPa to 7MPa is preferably used as the pressure range of the reaction. Under this pressure range, it is helpful to maintain the stability of the reaction medium and increase the reaction rate. Due to the high pressure and high temperature conditions, the hydroformylation reactor 1 needs to be made of high temperature resistant and high pressure resistant materials. The material of the hydroformylation reactor 1 in this embodiment can be stainless steel, alloy steel, etc., to ensure the strength and corrosion resistance of the hydroformylation reactor 1, which is not limited here. In order to cope with possible situations of excessive pressure or temperature, the hydroformylation reactor 1 is usually equipped with safety protection measures such as a safety valve and a pressure release device to prevent accidents.

[0062] In one embodiment of the present disclosure, the pore size of the gas distributor 12 is 1 μm to 100 μm.

[0063] The pore size of the gas distributor 12 is designed to be 1 μm to 100 μm, preferably 10 μm to 50 μm, which can ensure that the synthesis gas can be evenly dispersed in the reaction medium in the hydroformylation reactor 1 in the form of fine bubbles. By selecting an appropriate pore size, the size of the bubble can be controlled, thereby affecting the gas-liquid contact area. Smaller bubbles can provide a larger gas-liquid contact area, which helps to improve the reaction efficiency. Distributors of different pore sizes can be selected according to the specific reaction conditions and catalyst requirements. Fine bubbles can improve the reaction efficiency, and larger bubbles can reduce energy consumption. In addition, the appropriate pore size can also ensure good dispersion of the gas under high pressure, avoiding bubble aggregation or uneven distribution due to pressure fluctuations.

[0064] like Figure 1 As shown, in one embodiment of the present disclosure, the distillation device 5 includes a light-removing tower 51, a refining tower 52 and a heavy-removing tower 53, the light-removing tower 51 is connected to the gas-liquid separator 4, the refining tower 52 is connected to the light-removing tower 51, and the heavy-removing tower 53 is connected to the refining tower 52.

[0065] The distillation device 5 is composed of a plurality of towers, mainly including a light-removing tower 51, a refining tower 52 and a heavy-removing tower 53. These towers are connected in sequence to form a complete distillation system for gradually separating and purifying the fourth liquid phase generated by the hydroformylation reaction. Specifically, the light-removing tower 51 is mainly used to separate low-boiling light components from the fourth liquid phase, and these light components include alkanes and other low-boiling impurities, and the separated heavy components include alcohols and unreacted aldehydes. The refining tower 52 is used to further separate and purify the substances coming out of the bottom of the light-removing tower 51. In the refining tower 52, the unreacted aldehydes are output from the top of the refining tower 52 and transported to the hydrogenation reactor 3 for recycling, and the heavy alcohols are transported to the next separation unit. In the heavy-removing tower 53, the heavy alcohols are separated into high-carbon alcohols and heavy oils.

[0066] This multi-tower series distillation device 5 design allows the various components in the mixture to be gradually separated, and finally a high-purity target product is obtained. The operating conditions of each tower (such as temperature, pressure, reflux ratio, etc.) need to be optimized according to the properties of the specific components to ensure a better separation effect. Through such a distillation process, not only the purity of the product can be improved, but also the by-products or unreacted raw materials can be recovered and reused, thereby improving the economic benefits and environmental performance of the overall process.

[0067] The following experimental examples further illustrate the reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins provided by the present disclosure: Experimental Example 1 The hydroformylation reactor 1 does not use a bottom tube, and the synthesis gas is directly introduced to react at the liquid surface. After 3 hours of reaction, the conversion rate of the raw material long-chain olefin is 20.35%. Because the mass transfer efficiency between the reaction material and the synthesis gas at the gas-liquid interface is low, although the temperature and pressure conditions in the experiment have been met, the final reaction conversion rate is still low, as shown in Table 1.

[0068] Experimental Example 2 The experimental results of using a bottom tube inside the hydroformylation reactor 1 but not using an aeration head to disperse the synthesis gas. The gas is rushed into the reaction material through the bottom tube and contacts the material. After 3 hours of reaction, the conversion rate of the raw material is 60.74%. Although this scheme allows the synthesis gas to contact the reaction material directly, the contact area is limited due to the bubbling volume being limited by the pipeline diameter; and only the material near the bottom tube can be directly involved in the reaction, and the material far from this pipeline cannot be fully contacted. Therefore, after 3 hours of reaction, the raw material conversion efficiency is slightly improved compared to the scheme without the bottom tube, but this scheme still cannot make the long-chain olefin raw material react efficiently, as shown in Table 1.

[0069] Experimental Example 3 The experimental results of four gas distributors 12 with a size of 50*240mm and a pore size of 10μm are distributed inside the hydroformylation reactor 1. Under this scheme, the synthesis gas is fully distributed in the reaction raw materials through the gas distributor 12, and the gas particle size distributed by the gas distributor 12 is small, which greatly increases the contact area between the synthesis gas and the raw materials and increases the mass transfer efficiency. After 3 hours of reaction, the raw material conversion rate reached 99.54%, and basically all the raw materials reacted and converted into aldehydes or alcohols, as shown in Table 1.

[0070] Table 1

[0071] The present disclosure provides a reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins. By evenly arranging a plurality of gas distributors at the bottom of a hydroformylation reactor, the synthesis gas can be evenly dispersed in the reactor and fully contact with the reaction raw materials, thereby improving the mass transfer efficiency between gas and liquid and improving the conversion rate of the Fischer-Tropsch long-chain olefins.

[0072] It should be noted that, for the above-mentioned method embodiments, for the sake of simplicity of description, they are all expressed as a series of action combinations, but those skilled in the art should know that the present disclosure is not limited by the described action sequence, because according to the present disclosure, certain steps can be performed in other sequences or simultaneously. Secondly, those skilled in the art should also know that the embodiments described in the specification are all preferred embodiments, and the actions and modules involved are not necessarily required by the present disclosure.

[0073] In the above embodiments, the description of each embodiment has its own emphasis. For parts that are not described in detail in a certain embodiment, reference can be made to the relevant descriptions of other embodiments.

[0074] The preferred embodiments of the present disclosure disclosed above are only used to help explain the present disclosure. The optional embodiments do not describe all the details in detail, nor do they limit the disclosure to only the specific implementation methods described. Obviously, many modifications and changes can be made according to the content of the present disclosure. The present disclosure selects and specifically describes these embodiments in order to better explain the principles and practical applications of the present disclosure, so that those skilled in the art can well understand and use the present disclosure. The present disclosure is limited only by the claims and their full scope and equivalents.

Claims

1. A reaction system for preparing high-carbon alcohols from Fischer-Tropsch long-chain olefins, characterized in that: include: A hydroformylation reactor (1), wherein an air inlet pipeline (11) is arranged at the bottom of the hydroformylation reactor (1), and a plurality of gas distributors (12) are evenly arranged, the gas distributors (12) are connected to the air inlet pipeline (11), synthesis gas enters the gas distributor (12) from the air inlet pipeline (11), and is evenly diffused from the gas distributor (12) into the hydroformylation reactor (1), and the hydroformylation reactor (1) is used for reacting Fischer-Tropsch long-chain olefins with the synthesis gas to generate a first liquid phase; a rotary falling film evaporator (2), the rotary falling film evaporator (2) being connected to the hydroformylation reactor (1) and used for separating the first liquid phase into a second liquid phase and a third liquid phase; A hydrogenation reactor (3), wherein a connecting pipe is provided on the top of the rotary falling film evaporator (2), the connecting pipe being connected to the hydrogenation reactor (3), and the hydrogenation reactor (3) being configured to cause the second liquid phase to undergo a hydrogenation reaction to generate a fourth liquid phase; a gas-liquid separator (4), the gas-liquid separator (4) being connected to the hydrogenation reactor (3), the gas-liquid separator (4) being configured to separate the fourth liquid phase from the hydrogen in the fourth liquid phase; A distillation device (5), the distillation device (5) is connected to the gas-liquid separator (4), and the distillation device (5) is used to distill the fourth liquid phase into high-carbon alcohols and heavy oil fractions.

2. The reaction system according to claim 1, characterized in that: The gas distributor (12) comprises a gas distributor body (121) and a distributor interface (122); the gas distributor body (121) is connected to the gas inlet pipeline (11) via the distributor interface (122).

3. The reaction system according to claim 2, characterized in that: The gas inlet pipe (11) comprises at least a vertical portion (111) and a horizontal portion (112); one end of the vertical portion (111) is connected to the outside of the hydroformylation reactor (1), and the other end is connected to the horizontal portion (112); the horizontal portion (112) is horizontally arranged at the bottom of the hydroformylation reactor (1); and the gas distributors (12) are all connected to the horizontal portion (112).

4. The reaction system according to claim 3, characterized in that: The vertical portion (111) comprises at least two vertical sections and one bent section, and the bent section is arranged between the two vertical sections.

5. The reaction system according to claim 3, characterized in that: The gas distributors (12) are evenly distributed in the circumferential direction.

6. The reaction system according to claim 5, characterized in that: The gas distributor (12) is circumferentially arranged at the bottom of the hydroformylation reactor (1), and the distance between adjacent gas distributors (12) is equal to the radius of the gas diffusion range of each gas distributor (12).

7. The reaction system according to claim 1, characterized in that: The top of the hydroformylation reactor (1) is also provided with a temperature measuring port (13), and a temperature measuring tube (14) is also provided inside the reactor. The temperature measuring tube (14) passes into the interior of the hydroformylation reactor (1) through the temperature measuring port (13).

8. The reaction system according to claim 1, characterized in that: The hydroformylation reactor (1) is a high-pressure reactor. The temperature in the hydroformylation reactor (1) is 80° C. to 240° C., and the pressure is 2 MPa to 8 MPa.

9. The reaction system according to claim 1, characterized in that: The pore size of the gas distributor (12) is 1 μm to 100 μm.

10. The reaction system according to claim 1, characterized in that: The distillation device (5) comprises a light-removal tower (51), a refining tower (52) and a heavy-removal tower (53); the light-removal tower (51) is connected to the gas-liquid separator (4); the refining tower (52) is connected to the light-removal tower (51); and the heavy-removal tower (53) is connected to the refining tower (52).

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