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

Abstract

The utility model 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 higher-carbon alcohols from Fischer-Tropsch long-chain olefins. Background Art

[0002] As an important chemical raw material, higher alcohols are widely used in various industrial fields, such as the manufacture of daily chemical products, textile auxiliaries, and various synthetic materials. In the process of preparing higher alcohols from olefins, the hydroformylation reaction is a crucial step. It first converts the olefin into the corresponding aldehyde, which is then further converted into the higher alcohol through a hydrogenation reaction. This series of reactions is crucial for the production of products such as lubricant base oils, surfactants, plasticizers, and other fine chemicals. However, existing hydroformylation reactors often suffer from low mass transfer efficiency, resulting in low olefin conversion within the reactor, reducing reaction efficiency, reducing the yield of the final product, and increasing production costs. Utility Model Content

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

[0004] To achieve the above objectives, the present disclosure adopts the following technical solutions:

[0005] The present disclosure provides a reaction system for preparing higher alcohols from Fischer-Tropsch long-chain olefins, comprising:

[0006] A hydroformylation reactor, wherein an air inlet pipe is provided at the bottom of the hydroformylation reactor and a plurality of gas distributors are evenly arranged. The gas distributors are connected to the air inlet pipe. Synthesis gas enters the gas distributors from the air inlet pipe and is evenly diffused into the hydroformylation reactor from the gas distributors. The hydroformylation reactor is used to react Fischer-Tropsch long-chain olefins with the synthesis gas to generate a first liquid phase.

[0007] a rotary falling film evaporator, the rotary falling film evaporator being connected to the hydroformylation reactor and being used for separating the first liquid phase into a second liquid phase and a third liquid phase;

[0008] A hydrogenation reactor, wherein a connecting pipe is provided 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;

[0009] a gas-liquid separator, the gas-liquid separator being in communication with the hydrogenation reactor and configured to separate the fourth liquid phase from hydrogen in the fourth liquid phase;

[0010] A distillation device is connected to the gas-liquid separator and is used for distilling the fourth liquid phase into higher carbon alcohols and recombinant oil.

[0011] 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 pipe through the distributor interface.

[0012] 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.

[0013] 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.

[0014] In one embodiment of the present disclosure, the gas distributors are evenly distributed in the circumferential direction.

[0015] In one embodiment of the present disclosure, the gas distributors are 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.

[0016] 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.

[0017] 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.

[0018] In one embodiment of the present disclosure, the pore size of the gas distributor is 1 μm to 100 μm.

[0019] In one embodiment of the present disclosure, the distillation device includes a light removal tower, a refining tower and a heavy removal tower, the light removal tower is connected to the gas-liquid separator, the refining tower is connected to the light removal tower, and the heavy removal tower is connected to the refining tower.

[0020] The reaction system for preparing higher-carbon alcohols from Fischer-Tropsch long-chain olefins provided in the present disclosure 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 contacted 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.

[0021] 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

[0022] Figure 1 This is a schematic structural diagram of a reaction system for preparing higher alcohols from Fischer-Tropsch long-chain olefins provided in one embodiment of the present disclosure;

[0023] Figure 2 1 is a schematic structural diagram of a hydroformylation reactor provided in one embodiment of the present disclosure;

[0024] Figure 3 This is a schematic diagram of the specific structure of a gas distributor provided by an embodiment of the present disclosure;

[0025] Figure 4 is a distribution diagram of a gas distributor provided by an embodiment of the present disclosure;

[0026] Figure 5 This is a distribution diagram of a gas distributor provided in another embodiment of the present disclosure.

[0027] 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 unit; 51-lightness removal tower; 52-refining tower; 53-weight removal tower. DETAILED DESCRIPTION

[0028] Various exemplary embodiments of the present disclosure will now be described in detail with reference to the accompanying drawings. It should be noted that unless otherwise specifically stated, 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.

[0029] 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.

[0030] 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 part of the specification.

[0031] It should be noted that like reference numerals and letters refer to like items in the following figures, and therefore, once an item is defined in one figure, it need not be further discussed in subsequent figures.

[0032] The specific embodiments of the present disclosure are described below with reference to the accompanying drawings.

[0033] 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.

[0034] In this article, "first", "second", etc. are only used to distinguish each other, and do not indicate the importance and order, or the prerequisite for each other's existence.

[0035] 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.

[0036] The present disclosure provides a reaction system for preparing higher 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 provided 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, and 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 to react Fischer-Tropsch long-chain olefins with the synthesis gas to generate a first liquid phase; a 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 provided 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; a 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; a 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 recombinant oil.

[0037] The present disclosure provides a reaction system for preparing higher-carbon alcohols from Fischer-Tropsch long-chain olefins. By evenly arranging multiple gas distributors at the bottom of the hydroformylation reactor, the synthesis gas can be evenly dispersed in the reactor and fully contacted 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.

[0038] 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.

[0039] like Figure 1 As shown, the reaction system for preparing higher 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.

[0040] An air inlet pipe 11 is provided 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 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 reacting Fischer-Tropsch long-chain olefins with the synthesis gas to generate a first liquid phase.

[0041] Specifically, the inlet pipe 11 is the passage for syngas (typically containing carbon monoxide and hydrogen) to enter the hydroformylation reactor 1. Multiple gas distributors 12 are evenly arranged at the bottom of the hydroformylation reactor 1. Each gas distributor 12 is connected to the inlet pipe 11 and is provided with multiple small holes or slits. Syngas enters the multiple gas distributors 12 through the inlet pipe 11 and diffuses evenly into the hydroformylation reactor 1 through the small holes or slits of the multiple gas distributors 12. The evenly arranged gas distributors 12 at the bottom of the hydroformylation reactor 1 ensure sufficient contact between the syngas and the Fischer-Tropsch long-chain olefins, improving gas-liquid mass transfer efficiency and, therefore, reaction efficiency. In the hydroformylation reactor 1, the Fischer-Tropsch long-chain olefins react with the syngas in the presence of a catalyst to produce a first liquid phase, which comprises the generated aldehydes, the catalyst solution, and unreacted raw materials. In this embodiment, the catalyst in the catalyst solution can be a cobalt carbonyl compound, a rhodium compound, and / or complex, such as dicobalt octacarbonyl, cobalt diisooctoate, or rhodium acetylacetonate; the catalyst ligand can be selected from commonly used phosphine ligands such as BISBI, triphenylphosphine, and 4,5-bis(diphenylphosphine)-9,9-dimethylxanthene; and the catalyst solvent can be selected from one or more of ethanol, cyclohexane, toluene, or xylene, without limitation. In this embodiment, the Fischer-Tropsch long-chain olefins are olefins having greater than 10 carbon atoms. Due to their large molecular weight, these olefins diffuse slowly as reaction feedstocks. Therefore, multiple gas distributors 12 are evenly disposed at the bottom of the hydroformylation reactor 1 to improve the mass transfer efficiency between the Fischer-Tropsch long-chain olefins and the synthesis gas, thereby increasing the conversion rate of the Fischer-Tropsch long-chain olefins.

[0042] 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.

[0043] Specifically, the rotary falling film evaporator 2 is connected to the hydroformylation reactor 1 and is used to separate the first liquid phase produced by the hydroformylation reaction. Once the first liquid phase enters the rotary falling film evaporator 2, the rotating structure of the rotary falling film evaporator 2 causes the liquid to form a thin falling film, which then flows along the heated surface of the evaporator. During this process, the rotary falling film evaporator 2 maintains a pressure of 0.15 MPa and a temperature of 285°C. Due to the high thermal efficiency provided by the heated surface, the volatile components in the liquid evaporate rapidly, while the heavier non-volatile components remain in the evaporator as the third liquid phase.

[0044] The design of the rotary falling film evaporator 2 ensures uniform distribution and rapid renewal of the liquid film, improving heat transfer efficiency and evaporation rate while reducing the possibility of scaling. This effectively separates the first liquid phase into two parts: one is a vapor containing a high concentration of volatile components, which condenses to form a second liquid phase containing aldehydes; the other is a non-volatile component, or third liquid phase, containing the catalyst solution. This catalyst solution can be transported back to the hydroformylation reactor 1 via the rotary falling film evaporator 2 for recycling. This separation process effectively separates the reaction product from other components, facilitating further refinement and purification, ultimately yielding high-quality target chemicals.

[0045] 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 perform a hydrogenation reaction on the second liquid phase to generate a fourth liquid phase.

[0046] Specifically, a connecting pipe is installed at the top of the rotary falling film evaporator 2, which is connected to the hydrogenation reactor 3. In the hydrogenation reactor 3, the second liquid phase reacts with hydrogen gas in the presence of a catalyst. The presence of the catalyst accelerates the chemical bonding between hydrogen molecules and various components in the second liquid phase, prompting hydrogenation reactions among these components. Hydrogenation reactions can be used to reduce unsaturated bonds (such as double or triple bonds) or convert certain functional groups (such as nitro or carbonyl groups) into more stable structures, thereby generating new compounds.

[0047] After the hydrogenation reaction, the resulting product is a fourth liquid phase, which contains alcohols produced by the hydrogenation reaction. In this embodiment, a fixed-bed hydrogenation reactor 3 is used as the hydrogenation reactor 3. The conditions in hydrogenation reactor 3 (such as temperature, pressure, and catalyst type) can be adjusted according to the characteristics of the desired product to optimize the reaction selectivity and yield. In this embodiment, the reaction temperature in hydrogenation reactor 3 is 80°C to 199°C, and the reaction pressure is 3 MPa to 5 MPa. The continuous operation of the rotary falling film evaporator 2 and hydrogenation reactor 3 enables the efficient separation and conversion of complex mixtures, ultimately yielding the desired target chemical.

[0048] 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.

[0049] Specifically, in hydrogenation reactor 3, the second liquid phase reacts with hydrogen under the action of a catalyst to produce a new compound, the fourth liquid phase. During this process, unreacted hydrogen and other volatile byproducts remain with the liquid product. The fourth liquid phase exiting hydrogenation reactor 3 enters gas-liquid separator 4, where it settles to the bottom due to gravity. The lighter gas phase (primarily residual hydrogen and other volatile components) is discharged through the top outlet and re-enters hydrogenation reactor 3 for recycling.

[0050] 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 fed into subsequent processing units to achieve higher purity requirements.

[0051] The distillation device 5 is connected to the gas-liquid separator 4 and is used for distilling the fourth liquid phase into higher carbon alcohols and heavy oil.

[0052] Specifically, the distillation unit 5 is used to distill the fourth liquid phase into higher alcohols and heavy oil. Within the distillation unit 5, the components of the mixture are separated through repeated partial evaporation and condensation. At the top of the distillation unit 5, the light components with lower boiling points, namely higher alcohols, are collected; at the bottom of the distillation unit 5, the heavy oil with higher boiling points is collected.

[0053] The reaction system for preparing higher 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 Fischer-Tropsch long-chain olefins and reducing production costs.

[0054] 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 .

[0055] Specifically, the gas distributor 12 is a key component in the hydroformylation reactor 1, consisting of a gas distributor body 121 and a distributor interface 122. The gas distributor body 121 is the component that actually performs the gas distribution function, typically having a structure with multiple tiny holes or slits to ensure that the gas is evenly dispersed into the liquid within the reactor. The distributor interface 122 connects the gas distributor body 121 to the gas inlet pipe 11, and is used to introduce the synthesis gas transported from the gas inlet pipe 11 into the gas distributor body 121.

[0056] Through the connection between distributor interface 122 and inlet pipe 11, syngas can stably enter the gas distributor body 121 and be evenly released into the liquid in the reactor through the holes or slits in the body, helping to ensure uniform distribution of reactants in the reactor, thereby improving reaction efficiency. Uniform gas distribution can also avoid excessively high or low gas concentrations in local areas, preventing side reactions or product quality degradation caused by inconsistent reaction conditions.

[0057] 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.

[0058] 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 above, which can reduce the resistance when the gas enters and help the gas to be better distributed throughout the 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.

[0059] In one embodiment of the present disclosure, the vertical portion 111 includes at least two vertical segments and one bent segment, and the bent segment is disposed between the two vertical segments.

[0060] The vertical portion 111 of the gas inlet conduit 11 is configured to include at least two vertical sections and one curved section. This structure allows for more efficient gas flow guidance into the hydroformylation reactor 1 and helps reduce resistance and turbulence in gas flow. The first vertical section begins outside the hydroformylation reactor 1 and extends upward. The primary function of this vertical section is to draw syngas from the outside and guide it to the next section. The curved section, located between the two vertical sections, serves to connect the upper and lower vertical sections. The curved section can be L-shaped, U-shaped, or another shape, depending on actual needs and spatial layout, and is not limited here. The curved section design facilitates smooth changes in gas flow direction, reduces resistance during gas flow, and facilitates better control of the speed and direction of gas entering the hydroformylation reactor 1. The second vertical section extends upward from the curved section until it connects with the horizontal section 112. The design of this second vertical section further guides the gas and ensures a smooth transition to the horizontal section 112.

[0061] The design of two vertical sections and one curved section allows the gas to be distributed more evenly before entering the horizontal section 112, facilitating the subsequent operation of the gas distributor 12. Furthermore, the angle and position of the curved section can be flexibly adjusted according to the actual spatial layout, allowing the pipeline to adapt to different installation environments.

[0062] In one embodiment of the present disclosure, the gas distributors 12 are evenly distributed in the circumferential direction.

[0063] 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 tiny 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.

[0064] 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 to maintain the stability and controllability of the entire reaction process.

[0065] like Figures 4 and 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 .

[0066] Specifically, if Figures 4 and 5 As shown, taking the configurations of four and 42 gas distributors 12 as examples, the gas distributors 12 are distributed in a ring around the bottom of the hydroformylation reactor 1. This layout allows gas to be evenly released from all directions at 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 precisely cover the area surrounding it. The gas diffusion ranges of adjacent distributors are interconnected, achieving coverage of the bottom of the hydroformylation reactor 1 as much as possible with as few gas distributors 12 as possible. This ensures uniform distribution of gas across the entire bottom of the reactor, avoids localized uneven gas concentration, reduces reaction dead zones, and thus improves reaction uniformity and efficiency.

[0067] 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 interior of the hydroformylation reactor 1 through the temperature measuring port 13 .

[0068] Specifically, the temperature measuring port 13 is located at the top of the reactor and is used to insert a 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 changes 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. Detecting these problems in time can take measures to prevent accidents.

[0069] like Figure 2As shown, in one embodiment of the present disclosure, the hydroformylation reactor 1 is provided with a feed port 15, an air outlet 16, and a pressure gauge 17. These 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 add the necessary raw materials, such as Fischer-Tropsch long-chain olefins and catalysts, into the hydroformylation reactor 1. The feed port 15 is typically provided with a sealing cover or valve to prevent gas leakage when no raw materials are being added. During the addition of raw materials, it is necessary to ensure the safety of the feeding process and avoid the introduction of air or other impurities that may affect the reaction. The air outlet 16 is used to discharge gases from the hydroformylation reactor 1, including unreacted synthesis gas, by-product gases, and other volatile components. The pressure gauge 17 is used to monitor the pressure inside the hydroformylation reactor 1. The pressure gauge 17 allows real-time acquisition of pressure data within the hydroformylation reactor 1, which is crucial for controlling reaction conditions and ensuring the safe operation of the reactor. The pressure gauge 17 is typically connected to a pressure gauge or pressure sensor, which can convert pressure signals into easily readable data. The pressure tap 17 also requires good sealing to prevent gas leakage.

[0070] In one embodiment of the present disclosure, the hydroformylation reactor 1 is a high-pressure reactor, and the temperature inside the hydroformylation reactor 1 is 80° C. to 240° C., and the pressure is 2 MPa to 8 MPa.

[0071] The hydroformylation reactor 1 is a high-pressure reactor, and its operating conditions are generally carried out at relatively high temperatures and pressures to ensure that the reaction can proceed efficiently. The temperature range is 80°C to 240°C. In this embodiment, 160°C to 240°C is preferably used as the reaction temperature range. In this temperature range, the activity of the reactants is enhanced, the reaction rate is accelerated, and the selectivity and yield of the product are improved. The choice of temperature needs to be determined based on the specific catalyst type, reactant characteristics, and target product to achieve the best 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 thus the reaction rate can be accelerated. In this embodiment, 4MPa to 7MPa is preferably used as the reaction pressure range. In this pressure range, it helps 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 and high-pressure resistant materials. The materials 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.

[0072] In one embodiment of the present disclosure, the pore size of the gas distributor 12 is 1 μm to 100 μm.

[0073] 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 into the reaction medium in the hydroformylation reactor 1 in the form of fine bubbles. By selecting an appropriate pore size, the size of the bubbles 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 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.

[0074] like Figure 1 As shown, in one embodiment of the present disclosure, the distillation device 5 includes 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.

[0075] The distillation unit 5 is composed of multiple towers, primarily including a light-removal tower 51, a refining tower 52, and a heavy-removal 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-removal tower 51 primarily separates low-boiling light components from the fourth liquid phase, including alkanes and other low-boiling impurities. The separated heavy components include alcohols and unreacted aldehydes. The refining tower 52 is used to further separate and purify the substances exiting the bottom of the light-removal tower 51. In the refining tower 52, the unreacted aldehydes are removed from the top of the refining tower 52 and transported to the hydrogenation reactor 3 for recycling, while the heavy alcohols are transported to the next separation unit. In the heavy-removal tower 53, the heavy alcohols are separated into higher alcohols and heavy oils.

[0076] This multi-tower series distillation unit 5 design allows for the gradual separation of various components in a mixture, ultimately yielding a high-purity target product. The operating conditions of each tower stage (such as temperature, pressure, and reflux ratio) must be optimized based on the properties of the specific components to ensure optimal separation. This distillation process not only improves product purity but also allows for the recovery and reuse of byproducts and unreacted raw materials, thereby enhancing the overall process's economic efficiency and environmental performance.

[0077] The following experimental examples further illustrate the reaction system for preparing higher alcohols from Fischer-Tropsch long-chain olefins provided by the present disclosure:

[0078] Experimental Example 1

[0079] Hydroformylation Reactor 1 did not use a dip tube, and synthesis gas was directly introduced to react at the liquid surface. After 3 hours of reaction, the conversion rate of the raw long-chain olefins was 20.35%. Because the mass transfer efficiency between the reactants and the synthesis gas at the gas-liquid interface is low, although the temperature and pressure conditions were met in the experiment, the final reaction conversion rate was still low, as shown in Table 1.

[0080] Experimental Example 2

[0081] 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 comes into contact with 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 come into direct contact with the reaction material, the contact area is limited because the bubbling volume is limited by the pipe diameter; and only the material near the bottom tube can be directly involved in the reaction, and the material farther away from the pipe cannot be fully contacted. Therefore, after 3 hours of reaction, its 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.

[0082] Experimental Example 3

[0083] Experimental results show that four gas distributors 12, each measuring 50 x 240 mm and with a pore size of 10 μm, were installed within the hydroformylation reactor 1. This design allows the syngas to be fully distributed throughout the feedstock via the gas distributors 12. Furthermore, the fine particle size of the gas distributed by the gas distributors 12 significantly increases the contact area between the syngas and the feedstock, thereby improving mass transfer efficiency. After three hours of reaction, the feedstock conversion rate reached 99.54%, with virtually all of the feedstock reacting and converting into aldehydes or alcohols, as shown in Table 1.

[0084] Table 1

[0085]

[0086] The present disclosure provides a reaction system for preparing higher-carbon alcohols from Fischer-Tropsch long-chain olefins. By evenly arranging multiple gas distributors at the bottom of the hydroformylation reactor, the synthesis gas can be evenly dispersed in the reactor and fully contacted with the reaction raw materials, thereby improving the mass transfer efficiency between gas and liquid and increasing the conversion rate of Fischer-Tropsch long-chain olefins.

[0087] It should be noted that for the aforementioned method embodiments, for ease of description, they are all expressed as a series of action combinations, but those skilled in the art should be aware that the present disclosure is not limited by the order of the actions described, because according to the present disclosure, certain steps can be performed in other orders or simultaneously. Secondly, those skilled in the art should also be aware 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.

[0088] In the above embodiments, the description of each embodiment has its own focus. For parts that are not described in detail in a certain embodiment, reference can be made to the relevant descriptions of other embodiments.

[0089] The preferred embodiments of the present disclosure disclosed above are intended only to help illustrate the present disclosure. The optional embodiments do not describe all details in detail, nor do they limit the present disclosure to the specific embodiments described. Obviously, many modifications and variations can be made based on 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 better understand and utilize 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 higher alcohols from Fischer-Tropsch long-chain olefins, characterized in that: include: A hydroformylation reactor (1), wherein 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 thereon, wherein the gas distributors (12) are connected to the air inlet pipe (11), and synthesis gas enters the gas distributors (12) from the air inlet pipe (11) and is evenly diffused from the gas distributors (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 being 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) is connected to the gas-liquid separator (4), and the distillation device (5) is used to distill the fourth liquid phase into higher carbon alcohols and heavy oil.

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), and the gas distributor body (121) is connected to the gas inlet pipe (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 bending section, and the bending 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 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).

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 inside 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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