An apparatus and process for the production of aldehydes by olefin hydroformylation

Abstract

The application discloses an olefin hydroformylation aldehyde synthesis production device and process, comprising the following steps: (1) the raw material enters the bubble reactor of the reaction section of the reaction extraction rectifying tower and mixes with the catalyst, and carbon monoxide and hydrogen are introduced to carry out the hydroformylation reaction under high pressure; (2) the reaction product is overflowed to the rectifying section to carry out separation; (3) the alkanes byproduct and the olefin raw material with similar boiling points are separated through the eccentric rotating disc extraction tower of the extraction section of the reaction extraction rectifying tower; (4) the light components on the tower top are separated through the rectifying section; (5) the heavy components in the tower kettle are separated through the dividing wall column, and the aldehyde product is obtained through purification. The application adopts a new type of ionic liquid catalyst, separates the olefin and the alkane in the reaction extraction rectifying tower, improves the raw material utilization rate, simultaneously reduces the waste of the catalyst and the discharge of the raw material waste liquid, and increases the reaction conversion rate and the yield.

Description

Technical Field

[0001] This invention relates to the field of chemical preparation methods, specifically to a high-efficiency and energy-saving production apparatus and process for the hydroformylation of olefins to synthesize aldehydes. Background Technology

[0002] In the chemical industry, the hydroformylation of olefins and syngas to synthesize aldehydes is a very important production process. Currently, a mainstream process for the hydroformylation of olefins to synthesize aldehydes is as follows: olefin feedstock and syngas react at a pressure of 1-20 MPa and a temperature of 80-150℃ to obtain a reaction liquid containing unreacted olefin feedstock, alkane byproducts with the same number of carbon atoms as the feedstock, product aldehyde, alcohol, and heavy components. The reaction liquid undergoes a first-stage flash evaporation to remove dissolved syngas, and the liquid phase obtained from the flash evaporation is then separated in a separation unit to remove light and heavy components, yielding the product aldehyde.

[0003] This type of process has three main problems:

[0004] 1) Aldehyde products, unreacted olefins and by-product alkanes are taken out from bubble column reactors or batch reactors. It is necessary to add a light component removal tower to separate the light components from the products. During the reaction process, the products are not transferred in time and the reaction raw materials are not reused in time, resulting in low conversion rate and yield, which increases production cost.

[0005] 2) Olefin feedstocks and alkane byproducts with the same number of carbon atoms are collected as light components from the separation unit. Since their boiling points are very close, they are difficult to separate by conventional distillation. Moreover, the production and energy costs of separation by distillation and other methods are very high. The light components can only be treated as waste liquid, which will result in waste of raw materials and increased production costs.

[0006] 3) Commonly used hydroformylation of precious metal catalysts is taken out of the reactor along with the reaction products. To prevent the catalyst from being carried into the products, it is generally necessary to complex the catalyst to separate it. After the catalyst is complexed, wastewater will be generated that needs to be treated, and the catalyst will also be lost, which will also lead to waste of raw materials and increased production costs.

[0007] Therefore, it is still necessary to develop a new process for the hydroformylation of olefins to synthesize aldehydes to solve the problems existing in the current technology. Summary of the Invention

[0008] To overcome the shortcomings of the prior art, the present invention provides a production apparatus for the synthesis of aldehydes by hydroformylation of olefins, which couples extraction, distillation and reaction, thereby reducing equipment usage and energy consumption.

[0009] Another objective of this invention is to improve the process of olefin hydroformylation to aldehyde using the above-mentioned production apparatus. By separating olefins and alkanes in a reaction extraction distillation column, the utilization rate of raw materials is improved, the reaction conversion rate and yield are increased, and a novel ionic liquid catalyst is used to reduce catalyst waste and wastewater discharge.

[0010] To achieve the above-mentioned objectives, the technical solution adopted by this invention is as follows:

[0011] A production apparatus for the synthesis of aldehydes by hydroformylation of olefins, the production apparatus comprising a reactive extractive distillation column, which consists of a stripping section, a reaction section, an extraction section and a rectification section from bottom to top;

[0012] The reaction section is a partitioned tower structure. Distillation separation is carried out on the left side of the partition, and hydroformylation reaction is carried out on the right side of the partition. Preferably, multiple trays are set in the upper middle part of the right side of the partition, and raw material inlet and synthesis gas inlet are respectively set in the lower middle part and bottom of the right side of the partition, forming a plug flow bubbling reactor.

[0013] The extraction section is an eccentric rotating disk structure. An arc-shaped vertical baffle divides the extraction section into left and right sides. The left side of the baffle is the liquid phase clarification zone, and the eccentric rotating disk on the right side of the baffle is the gas-liquid mixing zone. An extractant inlet is located on the left side of the baffle at the top of the extraction section. The extractant can overflow into the right rotating disk and then return to the left side, where it undergoes multi-stage countercurrent extraction with the rising material at the bottom. The extracted phase flows from the left side of the bottom baffle to the reaction section.

[0014] In a preferred embodiment, the system further includes a flash tank, a gas-liquid separator, a light component separation tower, and a product refining tower. The inlet of the flash tank is connected to the top outlet of the reactive extractive distillation tower, the top outlet of the flash tank is connected to the inlet of the gas-liquid separator, the bottom outlet of the flash tank is connected to the inlet of the light component separation tower, the top gas phase outlet of the gas-liquid separator is connected to the syngas inlet of the reactive extractive distillation tower, the bottom liquid phase outlet of the gas-liquid separator is connected to the inlet of the light component separation tower, the inlet of the product refining tower is connected to the bottom outlet of the reactive extractive distillation tower, and the side-stream outlet of the product refining tower is connected to the extractant inlet of the reactive extractive distillation tower.

[0015] In one specific implementation, the left side of the reaction section partition has a length a1 of 0.7-5.6m, with 5-10mm holes spaced at equal intervals; the right side of the partition has a length b1 of 0.3-2.4m, with 1-3mm holes spaced at equal intervals to prevent the reaction liquid from flowing out from the bottom of the reaction section; the partition height c1 is 0.8-2.4m; the distance d1 from the top of the partition to the catalyst feed line is 0.5-1.5m; the distance e1 from the catalyst feed inlet to the reactant feed inlet is 0.2-0.6m; the distance f1 from the reactant feed inlet to the bottom of the reaction section is 0.1-0.3m; the distance from the partition to the catalyst feed inlet is 0.2-2.4m; the right side of the partition has 4-8 trays, with 1-3mm holes spaced at equal intervals on the trays;

[0016] Preferably, the reaction section is an elliptical cylinder, and a liquid distributor is provided on the top left side of the reaction section partition;

[0017] Preferably, the partition in the extraction section has no hole on the left side and a 1-3mm hole on the right side, and the turntable speed is 60-100rpm; the length a2 of the left side of the partition is 0.2-2m; the length b2 of the right side of the partition is 0.8-6m; and the spacing C2 between each partition in the extraction section is 0.2-0.6m.

[0018] On the other hand, a process for synthesizing aldehydes by hydroformylation of olefins is characterized by employing the aforementioned production apparatus and comprising the following steps:

[0019] 1) The raw material olefins enter the bubble reactor on the right side of the reaction section of the reaction extractive distillation column and are mixed with the catalyst. Syngas is then introduced to carry out the hydroformylation reaction under high pressure.

[0020] 2) The olefin formylation reaction product from step 1) overflows into the rectification section on the left side of the partition for separation. The light component evaporates to the extraction section, and the heavy component enters the stripping section.

[0021] 3) The light components from step 2) containing alkane byproducts and olefin feedstocks with similar boiling points enter the extraction section of the reactive extractive distillation column for extraction and separation.

[0022] 4) The light components separated from the extraction in step 3) enter the rectification section of the reactive extractive distillation column for further separation to obtain the light component feed stream at the top of the column, while the heavy components are returned to the extraction section for further extraction and separation;

[0023] 5) The heavy components from step 2) enter the stripping section of the reactive extractive distillation column for separation, and the bottom of the column yields a heavy component feed stream containing aldehyde products.

[0024] In a preferred embodiment, the light component material obtained from the top of the column in step 4) is flashed under reduced pressure in a flash tank, where the vapor and liquid are initially separated. After the vapor phase is cooled, it is further separated in a gas-liquid separator. The separated vapor phase is pressurized by a circulating compressor and then enters the bottom of the reactive extractive distillation column together with fresh syngas. The separated liquid phase enters the light component separation column for further separation.

[0025] Preferably, the recombinant feed stream of the aldehyde-containing product obtained from the bottom of the tower in step 5) enters the product refining tower after passing through the scraper reboiler. The product refining tower is a partitioned tower. The aldehyde product is obtained at the top of the tower, the extractant is obtained in the upper side stream, the condensed recombinant component is obtained in the lower side stream, and the catalyst is obtained in the bottom of the tower.

[0026] Preferably, the extractant and catalyst are discharged intermittently and replenished intermittently.

[0027] In one specific implementation, in step 1), the reaction raw materials are introduced from the lower right side of the partition and sprayed upward, the catalyst is introduced from the middle and lower right side of the partition and sprayed downward, and the synthesis gas enters through the small hole at the bottom right side of the partition.

[0028] Preferably, the extract phase entering the reaction section continues to separate on the left side of the partition and in the stripping section, the light olefin component enters the reaction section to continue participating in the reaction, and the heavy component is discharged from the bottom of the column;

[0029] Preferably, the syngas at room temperature enters from the bottom of the column, passes through the reaction section, and cools the reaction through throttling expansion and a large amount of circulating syngas, so that the reaction extractive distillation column maintains a good temperature gradient distribution.

[0030] Preferably, the raw material olefin is one or more of C4-C12 isoolefins, or one or more of C4-C12 isoolefins and a small amount of alkanes; preferably, the mass percentage of C4-C12 isoolefins is 80-95% and the mass percentage of alkanes is 5-20%.

[0031] In one specific embodiment, the catalyst is a noble metal homogeneous ionic liquid catalyst. Preferably, the noble metal is selected from at least one of cobalt, rhodium, ruthenium, and palladium, with palladium being the most preferred. The ligand is selected from any one of 2-(diphenylphosphine)pyridine, trifluoromethanesulfonic acid, methanesulfonic acid, toluenesulfonic acid, polysulfonic acid resin, butyl p-benzenesulfonate, and boric acid, with butyl p-benzenesulfonate being the most preferred. Preferably, the molar ratio of catalyst, ligand, and ionic liquid is 1:3:1 to 1:3:3, with 1:3:1 being the most preferred.

[0032] Preferably, the extractant is selected from one or more of ortho-, meta-, and dimethyl terephthalate, morpholine derivatives, sulfone derivatives, DMF, and C4-C16 nitrile, with dimethyl terephthalate being the most preferred.

[0033] In one specific implementation, the reactive extractive distillation column has a theoretical plate number of 30-100, preferably 60-70; a diameter of 1-8m, preferably 1-4m; a reflux ratio of 1-20, preferably 5-10; and a total pressure drop of 0.2-10 bar, preferably 1-5 bar.

[0034] In one specific embodiment, the amount of catalyst in the reaction solution is 1%-6% by mass, preferably 2%-4%; the reaction temperature is 120-220℃, preferably 150-200℃; the reaction pressure is 1-150 barA, preferably 10 bar-50 barA; the reaction residence time is 0.5-3h, preferably 1-2h; the pressure drop of the bubbling reactor is 0.1-2 bar, preferably 0.5-1.5 bar; and the ratio of hydrogen to CO in the synthesis gas is 1:0.5-2, preferably 1:1-1.5.

[0035] In one specific implementation, the theoretical plate number of the light component separation tower is 5-30, preferably 10-20; the reflux ratio is 0.5-10, preferably 5-10; the tower top pressure is 0.2-10 barA, preferably 0.2-5 barA; and the overall tower pressure drop is 1-10 kPa, preferably 1-5 kPa.

[0036] Preferably, the theoretical number of plates in the product refining tower is 20-50, more preferably 20-30; the reflux ratio is 0.5-5, more preferably 0.5-2; the tower top pressure is 1-10 kPaA, more preferably 1-5 kPaA; and the overall tower pressure drop is 0.5-5 kPa, more preferably 0.5-2 kPa.

[0037] Compared with the prior art, the present invention has the following beneficial effects:

[0038] (1) The process for synthesizing aldehydes in this invention involves a hydroformylation reaction on the right side of the reaction section partition and a distillation separation on the left side. Syngas enters through a small hole at the bottom of the right side of the partition. The reaction product obtained from the reaction on the right side of the partition overflows to the left side for distillation. The light components evaporate to the extraction section. The extract phase entering the reaction section is separated on the left side of the partition and in the stripping section. The olefins diffuse to the right side of the partition to continue the reaction, which improves the raw material utilization rate, reaction conversion rate and yield and reduces the discharge of raw material waste liquid. The heavy components flow into the stripping section, which can realize the separation of by-product alkanes and product aldehydes without the need for an additional light component removal tower to separate the two.

[0039] (2) In the process of synthesizing aldehydes of the present invention, the olefin raw materials with the same number of carbons produced by hydroformylation and the alkane byproducts are separated by extraction, which avoids the accumulation of alkane, greatly reduces energy consumption, reduces the discharge of light component waste liquid, avoids the loss of olefin raw materials caused by the discharge of alkane waste liquid, and the alkane light components are separated and utilized by light component separation tower.

[0040] (3) The process for synthesizing aldehydes in this invention uses homogeneous noble metal ionic liquid as a catalyst. The product, catalyst and extractant can be separated by a partition tower, avoiding separation by complexation removal, reducing the use of complexation tanks and wastewater treatment, and saving energy. Attached Figure Description

[0041] Figure 1 This is a schematic diagram of the apparatus system for the synthesis of aldehydes by hydroformylation of olefins according to the present invention.

[0042] Figure 2 This is a schematic diagram of the reaction section structure of the extraction reactive distillation column of the present invention.

[0043] Figure 3 This is a schematic diagram of the extraction section of the extraction reactive distillation column of the present invention.

[0044] Figure 4 This is a three-dimensional structural diagram of the extraction section of the extraction reactive distillation column of the present invention.

[0045] Among them, 1 is the reaction extraction distillation column, 2 is the stripping section, 3 is the reaction section, 4 is the extraction section, 5 is the rectification section, 6 is the fresh syngas, 7 is the syngas compressor, 8 is the condenser, 9 is the gas-liquid separator, 10 is the light component separation column, 11 is the product refining column, 12 is the scraped reboiler, 13 is the scraped liquid tank, 14 is the feed inlet, 15 is the fresh extractant, 16 is the fresh catalyst, 17 is the flare outlet, 18 is the small molecule alkane outlet, 19 is the product outlet, 20 is the condensed heavy component outlet, 21 is the other alkane outlet, 22 is the intermittent external discharge outlet, 23 is the rotary table, 24 is the horizontal baffle, 25 is the arc baffle, 26 is the outer shell, and 27 is the rotating shaft. Detailed Implementation

[0046] To better understand the technical solution of the present invention, the following embodiments will further illustrate the method provided by the present invention. However, the present invention is not limited to the listed embodiments, but should also include any other known modifications within the scope of the claims of the present invention.

[0047] like Figure 1As shown, a production apparatus for the hydroformylation of olefins to synthesize aldehydes includes a reactive extractive distillation column 1, a product purification column 11, and a light component separation column 10. The reactive extractive distillation column 1 consists of a stripping section 2, a reaction section 3, an extraction section 4, and a rectification section 5, arranged from bottom to top. Fresh syngas 6 is connected to the inlet of a syngas compressor 7 via pipeline. The outlets of the fresh syngas compressor 7 and the circulating syngas compressor 7 are connected to the bottom of the reactive extractive distillation column 1 via pipeline. The feed inlet 14 is connected to the reaction section 3 and flows into the right side of the partition of the reaction section 3. The top outlet of the reactive extractive distillation column 1 is connected to the feed inlet of a gas-liquid separator 9 via pipeline, resulting in a gas-liquid two-phase system. The gas phase enters the second gas-liquid separator 9 for further gas-liquid separation. Part of the gas phase is burned in a flare 17, and part is recycled back into the reactive extractive distillation column 1 from the syngas compressor 7. The liquid phase is separated from the light component at the outlet. The feed inlet of column 10 is connected to the light component separation column 10, which has a small molecule alkane outlet 18 at the top and other alkane outlets 21 at the bottom. The bottom outlet of the reaction extractive distillation column 1 is connected to the scraped reboiler 12 through a pipeline. The gas phase returns to the bottom of the reaction extractive distillation column 1, and the liquid phase enters the scraped lower liquid tank 13, and then enters the product purification column 11 for separation. The extractant collected from the upper side stream of the product purification column 11 is condensed by the condenser 8 and enters the extraction section 4 together with the fresh extractant 15. The catalyst collected from the bottom of the product purification column 11 enters the reaction section 3 together with the fresh catalyst 16. The bottom pipeline is also provided with an intermittent external discharge port 22. The top of the column has a product outlet 19, and the lower side stream has a condensation heavy component outlet 20.

[0048] like Figure 2 As shown, the reaction section 3 is a partition tower structure. Distillation separation is carried out on the left side of the partition, and hydroformylation reaction is carried out on the right side of the partition. Preferably, multiple trays are set in the middle and upper part of the right side of the partition, and raw material inlet and synthesis gas inlet are respectively provided in the middle and lower part and bottom of the right side of the partition, forming a plug flow bubbling reactor.

[0049] Specifically, reaction section 3 consists of two parts, separated at the left end by an arc-shaped partition. The left side of the partition is for distillation, and the right side is for hydroformylation. To improve conversion and yield, a multi-layer tray is installed in the upper middle part of the right side of the partition, which is equivalent to a plug flow bubble column reactor. The reactant 14 is introduced from the lower right side of the partition and sprayed upwards, while the catalyst is introduced from the lower middle part of the right side of the partition and sprayed downwards. Syngas enters through a small hole at the bottom of the right side of the partition and undergoes hydroformylation in this area. The reaction product obtained from the reaction on the right side of the partition overflows to the left side for distillation. The light components evaporate to the extraction section 4, while the heavy components flow into the stripping section 2. The extract phase entering reaction section 3 is separated on the left side of the partition and in the stripping section 2. The olefin diffuses from the upper and lower parts of the right side of the partition to the right side of the partition to continue the reaction.

[0050] Furthermore, the left side a1 of the partition in reaction section 3 has a length of 0.7-5.6m and is perforated with 5-10mm holes at equal intervals, allowing for mass and heat transfer between vapor and liquid. The right side b1 of the partition has a length of 0.3-2.4m and is perforated with 1-3mm holes at equal intervals to prevent the reaction liquid from flowing out from the bottom of the reaction section. The height c1 of the partition is 0.8-2.4m to provide sufficient residence time for the reaction. The distance d1 from the top of the partition to the catalyst feed line is 0.5-1.5m. The distance e1 from the catalyst feed inlet to the reactant feed inlet is 0.2-0.6m. The distance f1 from the reactant feed inlet to the bottom of the reaction section is 0.1-0.3m. The distance from the partition to the catalyst feed inlet is 0.2-2.4m. There are 4-8 trays on the right side of the partition, with 1-3mm holes perforated at equal intervals on the trays. Reaction section 3 is made into an elliptical cylinder to increase the residence time. A liquid distributor is installed at the top left side of the partition in reaction section 3 to facilitate the extraction of olefins by the extractant.

[0051] like Figure 3 As shown, the extraction section 4 is an eccentric rotating disk structure. An arc-shaped vertical partition divides the extraction section 4 into left and right sides. The left side of the partition is the liquid phase clarification zone, and the eccentric rotating disk is on the right side of the partition, which is the gas-liquid mixing zone. An extractant inlet is provided on the left side of the partition at the top of the extraction section. The extractant can overflow into the right rotating disk and then return to the left side to perform multi-stage countercurrent extraction with the rising material at the bottom. The extracted phase flows from the left side of the bottom partition to the reaction section 3.

[0052] Specifically, such as Figure 4 As shown, the extraction section 4 is an eccentric rotating disk enclosed by the outer shell 26. An arc-shaped baffle 25 divides it into left and right sides. The left side of the baffle is not perforated, while the right side has a 1-3mm perforation, which facilitates mass transfer of the syngas during extraction. The rotating disk 23 is driven by the rotating shaft 27 to rotate at a speed of 60-100 rpm. The extractant is fed from the top of the extraction section 4, with the inlet on the left side of the baffle. It overflows into the right rotating disk, where it undergoes multi-stage countercurrent extraction with the rising light components at the bottom. Guided by the right baffle 24, it flows back to the left baffle 24, continuing this continuous flow. The extracted phase flows from the left side of the bottom baffle to the reaction section 3. The length of the arc-shaped baffle 25 on the left side (a2) of the extraction section 4 is 0.2-2m; the length of the arc-shaped baffle on the right side (b2) is 0.8-6m; and the spacing between the baffles in each section of the extraction section 4 (C2) is 0.2-0.6m.

[0053] On the other hand, a process for synthesizing aldehydes by hydroformylation of olefins includes the following steps:

[0054] (1) The raw material enters the bubbling reactor of the reaction section of the reaction extraction distillation column and is mixed with the catalyst. Carbon monoxide and hydrogen are introduced to carry out the hydroformylation reaction under high pressure.

[0055] (2) The reaction products overflow into the rectification section on the left side of the partition for separation;

[0056] (3) Alkane byproducts and olefin feedstocks with similar boiling points are extracted and separated by an eccentric rotating disc extractor in the extraction section of a reaction extraction distillation column.

[0057] (4) The light components at the top of the column are separated through the rectification section;

[0058] (5) The heavy components in the bottom of the tower are separated by the adjacent tower and further purified by the stripping section to obtain aldehyde products.

[0059] The raw material is one or more C4-C12 isoolefins, and may also contain a small amount of alkanes, for example, the mass percentage of C4-C12 isoolefins is 80-95% and the mass percentage of alkanes is 5-20%.

[0060] The catalyst for the hydroformylation reaction is a noble metal homogeneous ionic liquid catalyst, wherein the noble metal includes cobalt, rhodium, ruthenium, and palladium, with palladium being preferred; the ligands used in the ionic liquid include 2-(diphenylphosphine)pyridine, trifluoromethanesulfonic acid, methanesulfonic acid, toluenesulfonic acid, polysulfonic acid resin, butyl p-benzenesulfonate, boric acid, etc., with butyl p-benzenesulfonate being preferred. The amount of catalyst in the reaction solution is 1%-6% by mass, for example, including but not limited to 2%, 3%, 4%, 5%, and 6%, preferably 2%-4%. The molar ratio of catalyst, ligand, and ionic liquid is 1:3:1 to 1:3:3, for example, including but not limited to 1:3:1, 1:3:2, and 1:3:3, preferably 1:3:1.

[0061] The theoretical plate number of the reactive extractive distillation column is 30-100, including but not limited to 40, 50, 60, 70, 80, and 90, preferably 60-70; the diameter is 1-8m, including but not limited to 2m, 3m, 4m, 5m, 6m, and 7m, preferably 1-4m; the reflux ratio is 1-20, including but not limited to 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, and 19, preferably 5-10; the overall pressure drop is 0.2-10 bar, including but not limited to 1 bar, 2 bar, 3 bar, 4 bar, 5 bar, 6 bar, 7 bar, 8 bar, and 9 bar, preferably 1-5 bar.

[0062] The reaction temperature in the reaction section is 120-220℃, including but not limited to 130℃, 140℃, 150℃, 160℃, 170℃, 180℃, 190℃, 200℃, and 210℃, preferably 150-200℃; the reaction pressure is 1-150 barA, including but not limited to 5 barA, 10 barA, 15 barA, 20 barA, 25 barA, 30 barA, 35 barA, 40 barA, 45 barA, 50 barA, 55 barA, 60 barA, 65 barA, 70 barA, 80 barA, 90 barA, 100 barA, 110 barA, 120 barA, 130 barA, 140 barA, and 145 barA, preferably 10 barA-50 barA; the reaction residence time is 0.5-3 hours, including but not limited to 1 hour, 1 minute... The time is 0.5h, 2h, 2.5h, preferably 1-2h; the pressure drop of the bubbling reactor is 0.1-2bar, for example, including but not limited to 0.2bar, 0.3bar, 0.4bar, 0.5bar, 0.6bar, 0.7bar, 0.8bar, 0.9bar, 1bar, 1.1bar, 1.2bar, 1.3bar, 1.4bar, 1.5bar, 1.6bar, 1.7bar, 1.8bar, 1.9bar, 2bar, preferably 0.5-1.5bar; the ratio of hydrogen to CO in the synthesis gas is 1:0.5 to 2, for example, including but not limited to 1:0.6, 1:0.7, 1:0.8, 1:0.9, 1:1, 1:1.1, 1:1.2, 1:1.3, 1:1.4, 1:1.5, 1:1.6, 1:1.7, 1:1.8, 1:1.9, preferably 1:1-1.5.

[0063] The extractant includes one or more of the following: ortho-, meta-, and dimethyl terephthalate, morpholines, sulfones, DMF, and C4-C16 nitrile, preferably dimethyl terephthalate. The morpholines are selected from any one of morpholine, N-ethylmorpholine, N-(2-hydroxypropyl)morpholine, 4-[2-(dimethylamino)ethyl]morpholine, and tridecamorpholine; the sulfones are selected from sulfolane, diethyl sulfone, diphenyl sulfone, phenylethyl sulfone, etc., but not limited thereto; the C4-C16 nitrile is selected from any one of cyclopropionitrile, pentacyanide, 5-hexanolynitrile, benzonitrile, 4-methylbenzonitrile, cinnamonitrile, undecanolynitrile, dodecacyanide, tridecacyanide, tetradecacyanide, pentadecanolynitrile, and hexadecanolynitrile, but not limited thereto. The mass ratio of the extractant to the reactants is 1:1-5, for example, including but not limited to 1:1, 1:2, 1:3, 1:4, and 1:5, preferably 1:2-1:3.

[0064] In this process, the material from the reaction section continues to be separated in the stripping section, the light olefin components enter the reaction section to continue to participate in the reaction, and the heavy components are discharged from the bottom of the column; the syngas at room temperature enters from the bottom of the column, passes through the reaction section, and cools the reaction through throttling expansion and a large amount of circulating syngas, so that the reaction extractive distillation column maintains a good temperature gradient distribution and avoids temperature inversion.

[0065] In the reactive extractive distillation column, the overhead material undergoes vacuum flash evaporation to separate the vapor and liquid phases. After cooling, the vapor phase is further separated in a gas-liquid separator. The vapor phase is then pressurized by a circulating compressor and enters the bottom of the reactive extractive distillation column along with fresh syngas. The liquid phase enters a light component separation column for further separation. Small molecule hydrocarbons are obtained at the top of the column, and alkanes with the same carbon number as the olefin feedstock are obtained at the bottom. The bottom material of the reactive extractive distillation column passes through a scraped reboiler and enters a product purification column. This product purification column is a partitioned column. Aldehydes are obtained at the top, the extractant is obtained from the upper side stream, condensed heavy components are obtained from the lower side stream, and the catalyst is obtained from the bottom. The extractant and catalyst are intermittently discharged and intermittently fed.

[0066] Specifically, the theoretical plate number of the light component separation column is 5-30, for example, including but not limited to 6, 7, 8, 9, 10, 11, 15, 18, 20, 25, 26, 28, 29, preferably 10-20; the reflux ratio is 0.5-10, for example, including but not limited to 1, 2, 3, 4, 5, 6, 7, 8, 9, preferably 5-10; the column top pressure is 0.2-10 barA, for example, including but not limited to 0.2 barA, 0.5 bar, 0.8 barA, 1 barA, 2 barA, 3 barA, 4 barA, 5 barA, 6 barA, 7 barA, 8 barA, 9 barA, preferably 0.2-5 barA; the overall column pressure drop is 1-10 kPa, for example, including but not limited to 1.5 kPa, 2 kPa, 2.5 kPa, 3 kPa, 3.5 kPa, 4 kPa, 4.5 kPa, preferably 1-5 kPa.

[0067] The theoretical plate number of the product refining column is 20-50, including but not limited to 20, 25, 30, 35, 40, and 45, preferably 20-30; the reflux ratio is 0.5-5, including but not limited to 0.5, 1, 2, 3, 4, and 5, preferably 0.5-2; the column top pressure is 1-10 kPaA, including but not limited to 1.5 kPaA, 2 kPaA, 2.5 kPaA, 3 kPaA, 3.5 kPaA, 4 kPaA, and 4.5 kPaA, preferably 1-5 kPaA; the overall column pressure drop is 0.5-5 kPa, including but not limited to 1 kPa, 1.5 kPa, 2 kPa, 2.5 kPa, 3 kPa, 3.5 kPa, 4 kPa, and 4.5 kPa, preferably 0.5-2 kPa.

[0068] The present invention will now be described in detail with reference to more specific embodiments, but this does not constitute any limitation.

[0069] The theoretical plate number of the reactive extractive distillation column used in the example is 70, the column diameter is selected as 2m, the reflux ratio is 8, the total column pressure is 4MPaA, and the total column pressure is 2bar due to the high pressure drop in the reaction section and the extraction section.

[0070] Preparation Example 1: Preparation of Homogeneous Noble Metal Ionic Liquid Catalysts

[0071] Ionic liquid preparation: Toluene, butyl p-benzenesulfonate, and 1-methylimidazole were added to a beaker at a mass ratio of 4:3:1 and refluxed under a nitrogen atmosphere for 24 h until the reaction liquid separated into layers. The toluene layer was removed, and the ionic liquid layer was washed three times with n-hexane. Pd catalyst preparation: 1 g of PdCl3·H2O was placed in a container, CO was introduced, and the container was placed in an 80 °C oil bath. Then, 3 g of BaCO3 was added, and 20 ml of petroleum ether was added under a nitrogen atmosphere. The mixture was refluxed under a nitrogen atmosphere for 48 h and washed with petroleum ether to obtain the catalyst.

[0072] Ligand preparation: At -50℃, 10 mmol of toluenesulfonic acid and methyl trifluoromethanesulfonate were added to 50 ml of dichloromethane solution containing 5 mmol of 1,3,5-tris(p-imidazolylphenyl)benzene. After removing the dichloromethane, the solution was washed with anhydrous ethanol. The PD catalyst, ligand, and ionic liquid were mixed in a molar ratio of 1:3:1 to prepare a homogeneous PD metal ionic liquid catalyst, which was an oily liquid.

[0073] Preparation Example 2: Preparation of Homogeneous Noble Metal Ionic Liquid Catalysts

[0074] The catalyst was prepared using the same method as in Preparation Example 1.

[0075] Ionic liquid preparation: Toluene, butyl p-benzenesulfonate, and 1-methylimidazole were added to a beaker at a mass ratio of 4:3:1 and refluxed under a nitrogen atmosphere for 24 h until the reaction liquid separated into layers. The toluene layer was removed, and the ionic liquid layer was washed three times with n-hexane. Co catalyst preparation: 1 g of CoCl3·H2O was placed in a container, CO was introduced, and the container was placed in an 80 °C oil bath. Then, 3 g of BaCO3 was added, and 20 ml of petroleum ether was added under a nitrogen atmosphere. The mixture was refluxed under a nitrogen atmosphere for 48 h and washed with petroleum ether to obtain the catalyst.

[0076] Ligand preparation: At -50℃, 10 mmol of boric acid and polysulfonic acid resin were added to 50 ml of dichloromethane solution containing 5 mmol of 1,3,5-tris(p-imidazolylphenyl)benzene. After removing the dichloromethane, the solution was washed with anhydrous ethanol. The PD catalyst, ligand, and ionic liquid were mixed in a molar ratio of 1:3:2 to prepare a homogeneous PD metal ionic liquid catalyst, which was an oily liquid.

[0077] Preparation Example 3: Preparation of Homogeneous Noble Metal Ionic Liquid Catalysts

[0078] The catalyst was prepared using the same method as in Preparation Example 1.

[0079] Ionic liquid preparation: Toluene, butyl p-benzenesulfonate, and 1-methylimidazole were added to a beaker at a mass ratio of 4:3:1 and refluxed under a nitrogen atmosphere for 24 h until the reaction liquid separated into layers. The toluene layer was removed, and the ionic liquid layer was washed three times with n-hexane. Rh catalyst preparation: 1 g of RhCl3·H2O was placed in a container, CO was introduced, and the container was placed in an 80 °C oil bath. Then, 3 g of BaCO3 was added, and 20 ml of petroleum ether was added under a nitrogen atmosphere. The mixture was refluxed under a nitrogen atmosphere for 48 h and washed with petroleum ether to obtain the catalyst.

[0080] Ligand preparation: At -50℃, 10 mmol of methanesulfonic acid, butyl p-benzenesulfonate, and 2-(diphenylphosphine)pyridine were added to 50 ml of dichloromethane solution containing 5 mmol of 1,3,5-tris(p-imidazolylphenyl)benzene. The dichloromethane was removed, and the solution was washed with anhydrous ethanol. The PD catalyst, ligand, and ionic liquid were mixed in a molar ratio of 1:3:3 to prepare a homogeneous PD metal ionic liquid catalyst, which was an oily liquid.

[0081] Example 1

[0082] Using diisobutylene (DIB) as raw material (DIB content > 99.7%), the raw material enters from the reaction section at a flow rate of 3000 kg / h. Synthesis gas is introduced from the bottom of the reactive extractive distillation column. A baffle is added in the middle of the reaction section to facilitate simultaneous reaction and separation. The hydroformylation reaction takes place on the right side of the baffle in the reaction section of the reactive extractive distillation column. The height of the baffle, c1, is 1.6 m, and the length of the right side of the baffle, b1, is 0.5 m. 2 mm holes are opened at equal intervals to allow the synthesis gas to rise while preventing the reaction liquid from falling. The distance from the top of the baffle to the catalyst feed line, d1, is 1 m. The distance from the catalyst inlet to the reactant feed inlet, e1, is 0.4 m. The distance from the reactant feed inlet to the bottom of the reaction section, f1, is 0.2 m. The distance from the baffle to the catalyst inlet is 1.3 m. There are 6 trays on the right side of the baffle, and 2 mm holes are opened at equal intervals on the trays. The main reaction is the reaction of DIB with syngas to produce isononanal, and the side reaction is the hydrogenation of DIB to produce isononane, as well as a small amount of isononanal and isononanal condensation to form a heavy component. A Pd metal ionic liquid catalyst (Preparation Example 1) was used as the catalyst, with a catalyst mass ratio of 3% in the reaction solution. The reaction temperature was 180℃, the reaction pressure was 4 MPaA, the DIB conversion rate was 99.5%, and the isononanal yield was 99%. The reaction solution overflowed into the left-side rectification section. The left side of the reaction section partition a1 has a length of 1.5 m and is equidistantly perforated with 8 mm holes. The light component went to the extraction section. After extraction, the extractant entered the reaction section, and the extractant separated from DIB and continued the reaction.

[0083] The syngas and light components of the reaction liquid from the reaction section enter the extraction section together. The hydrogen to CO ratio in the syngas is 1:1. Dimethyl terephthalate is used as the extractant. The extractant and light components undergo multi-stage countercurrent extraction in the extraction section. The mass ratio of dimethyl terephthalate to the reactants is 1:2. The rotary table rotates at 80 rpm, ensuring sufficient contact between the extractant and light components on the rotary table. The raffinate, isononane, and small molecule hydrocarbons enter the rectification section for further purification to remove the heavy components entrained in the extraction section. The left side (a2) of the arc-shaped partition in the extraction section is 0.5 m long and has no holes on the left side; the right side (b2) of the arc-shaped partition is 1.5 m long and has equidistant 2 mm holes, which is beneficial for increasing the mass transfer effect of the syngas extraction. The spacing (C2) between the partitions in each section of the extraction section is 0.4 m.

[0084] The composition of the top and bottom feeds from the reactive extractive distillation column was analyzed. The top flow rate was 17 kg / h, and the composition was 90% isononane and 10% other components. The bottom flow rate was 5355 kg / h, and the composition was 68% isononal, 28% dimethyl terephthalate, 2.3% macromolecular condensates, and 1.7% catalyst. The scraper used for bottom collection provided a heat source of S10 steam, and the vaporization rate was controlled to prevent the bottom feed from containing light components such as DIB.

[0085] The overhead feed from the reactive extractive distillation column undergoes vacuum flash evaporation to separate the vapor and liquid phases. After cooling, the vapor phase is further separated in a gas-liquid separator. Due to the discrepancy between the proportion of syngas discharged from the reaction and the proportion of fresh syngas, a small portion of the vapor phase is burned in the flare, while the majority is pressurized by the circulating compressor and enters the bottom of the reactive extractive distillation column along with the fresh syngas. The liquid phase enters the light component separation column for further separation. Small molecule hydrocarbons are obtained at the top, and alkanes with the same carbon number as the olefin feedstock are obtained at the bottom. The light component separation column has a theoretical plate number of 15, a reflux ratio of 0.6, and a top pressure of 3 barA; the overall pressure drop is 5 kPa. Analysis of the composition of the top and bottom feeds from the light component separation column reveals the following: Top flow rate: 1.6 kg / h; Top composition: 99.5% small molecule hydrocarbons, 0.5% others; Bottom flow rate: 15.4 kg / h; Bottom composition: 99% isononane, 1% others.

[0086] The feed from the bottom of the reactive extractive distillation column passes through a scraped reboiler and then enters the product purification column, which is a partitioned column. The aldehyde product is obtained at the top, the extractant is obtained from the upper side stream, the condensed heavy components are obtained from the lower side stream, and the catalyst is obtained from the bottom. The extractant and catalyst are intermittently discharged and intermittently fed. The product purification column has a theoretical plate number of 25, a reflux ratio of 1, a top pressure of 3 kPaA, and a total pressure drop of 1 kPa. The composition of the top and bottom feeds from the product refining tower was analyzed. The top flow rate was 3772.5 kg / h, and the top composition was 99.8% isononanal and 0.2% other components. The upper side stream flow rate was 1507.5 kg / h, and the upper side stream composition was 99.5% dimethyl terephthalate and 0.5% other components. The lower side stream flow rate was 123 kg / h, and the lower side stream composition was 98% condensed heavy components and 2% other components. The bottom flow rate was 92 kg / h, and the bottom composition was 99% Pd metal ion liquid catalyst and 1% other components.

[0087] Example 2

[0088] The same synthesis process and raw materials as in Example 1 were used, the main difference being that...

[0089] (1) Tridecanoic acid was used as the extractant;

[0090] (2) The left side of the reaction section partition is 0.7m long (a1), with 5mm holes at equal intervals; the right side of the partition is 0.3m long (b1), with 1mm holes at equal intervals; the partition height (c1) is 0.8m; the distance from the top of the partition to the catalyst feed line (d1) is 0.5m; the distance from the catalyst feed inlet to the reactant feed inlet (e1) is 0.2m; the distance from the reactant feed inlet to the bottom of the reaction section (f1) is 0.1m; the distance from the partition to the catalyst feed inlet is 0.2m; there are 4 trays on the right side of the partition, with 1mm holes at equal intervals on the trays.

[0091] (3) A 1mm hole is made on the right side of the partition, and the turntable speed is 60rpm; the length a2 of the left side of the partition is 0.2m; the length b2 of the right side of the partition is 0.8m; the spacing C2 between each partition in the extraction section is 0.2m;

[0092] (4) The raw material flow rate is 750 kg / h, and the other conditions are the same as in Example 1.

[0093] The final DIB conversion rate was 99.4%, and the isononal yield was 99%.

[0094] The composition of the top and bottom feeds from the light component separation tower was analyzed. The top flow rate was 0.4 kg / h, and the top composition was 99.6% small molecule hydrocarbons and 0.4% other components. The bottom flow rate was 3.9 kg / h, and the bottom composition was 99.1% isononane and 0.9% other components.

[0095] The composition of the top and bottom feeds from the product refining tower was analyzed. The top flow rate was 943.1 kg / h, and the top composition was 99.8% isononanal and 0.2% other components. The upper side stream flow rate was 376.8 kg / h, and the upper side stream composition was 99.6% dimethyl terephthalate and 0.4% other components. The lower side stream flow rate was 31 kg / h, and the lower side stream composition was 98% condensed heavy components and 2% other components. The bottom flow rate was 92 kg / h, and the bottom composition was 99% Pd metal ion liquid catalyst and 1% other components.

[0096] Example 3

[0097] The same synthesis process and raw materials as in Example 1 were used, the main difference being that...

[0098] (1) Tridemorpholine was used as the extractant;

[0099] (2) The left side of the reaction section partition is 5.6m long (a1), with 10mm holes at equal intervals; the right side of the partition is 2.4m long (b1), with 3mm holes at equal intervals; the partition height (c1) is 2.4m; the distance from the top of the partition to the catalyst feed line (d1) is 1.5m; the distance from the catalyst feed inlet to the reactant feed inlet (e1) is 0.6m; the distance from the reactant feed inlet to the bottom of the reaction section (f1) is 0.3m; the distance from the partition to the catalyst feed inlet is 2.4m; there are 8 trays on the right side of the partition, with 3mm holes at equal intervals on the trays.

[0100] (3) A 3mm hole is made on the right side of the partition, and the turntable speed is 100rpm; the length a2 on the left side of the partition is 2m; the length b2 on the right side of the partition is 6m; the spacing C2 between each partition in the extraction section is 0.6m;

[0101] (4) The raw material flow rate is 48,000 kg / h, and the other conditions are the same as in Example 1.

[0102] The final DIB conversion rate was 99.6%, and the isononal yield was 99.1%.

[0103] The composition of the top and bottom feeds from the light component separation tower was analyzed. The top flow rate was 19.2 kg / h, and the top composition was 99.6% small molecule hydrocarbons and 0.4% other components. The bottom flow rate was 187.2 kg / h, and the bottom composition was 99.1% isononane and 0.9% other components.

[0104] The composition of the top and bottom feeds from the product refining tower was analyzed. The top flow rate was 42568.8 kg / h, and the composition was: isononanal 99.9%, other components 0.1%. The upper side stream flow rate was 18086.4 kg / h, and the composition was: dimethyl terephthalate 99.7%, other components 0.3%. The lower side stream flow rate was 1488 kg / h, and the composition was: condensed heavy components 98.1%, other components 1.9%. The bottom flow rate was 4416 kg / h, and the composition was: Pd metal ion liquid catalyst 99%, other components 1%.

[0105] Example 4

[0106] The same synthesis process and raw materials as in Example 1 were used. The main difference was that the catalyst used was the Co catalyst prepared in Preparation Example 2, and DMF was used as the extractant. The other conditions were the same as in Example 1.

[0107] The final DIB conversion rate was 97%, and the isononal yield was 95%.

[0108] The composition of the top and bottom feeds from the light component separation tower was analyzed. At a top flow rate of 2 kg / h, the top composition was 99.3% small molecule hydrocarbons and 0.7% other components. At a bottom flow rate of 17 kg / h, the bottom composition was 98.9% isononane and 1.1% other components.

[0109] The composition of the top and bottom feeds from the product refining tower was analyzed. The top flow rate was 3702 kg / h, and the top composition was 99.6% isononanal and 0.4% other components. The upper side stream flow rate was 1501 kg / h, and the upper side stream composition was 99.5% dimethyl terephthalate and 0.5% other components. The lower side stream flow rate was 125 kg / h, and the lower side stream composition was 98% condensed heavy components and 2% other components. The bottom flow rate was 94 kg / h, and the bottom composition was 98.9% Pd metal ion liquid catalyst and 1.1% other components.

[0110] Example 5

[0111] The same synthesis process and raw materials as in Example 1 were used. The main difference was that the catalyst used was the Rh catalyst prepared in Preparation Example 3, and diphenyl sulfone was used as the extractant. The other conditions were the same as in Example 1.

[0112] The final DIB conversion rate was 97%, and the isononal yield was 94%.

[0113] The composition of the top and bottom feeds from the light component separation tower was analyzed. The top flow rate was 2.1 kg / h, and the top composition was 99.4% small molecule hydrocarbons and 0.6% other components. The bottom flow rate was 17.2 kg / h, and the bottom composition was 98.8% isononane and 1.2% other components.

[0114] The composition of the top and bottom feeds from the product refining tower was analyzed. The top flow rate was 3690 kg / h, and the top composition was 99.5% isononanal and 0.5% other components. The upper side stream flow rate was 1490 kg / h, and the upper side stream composition was 99.5% dimethyl terephthalate and 0.5% other components. The lower side stream flow rate was 126 kg / h, and the lower side stream composition was 98% condensed heavy components and 2% other components. The bottom flow rate was 95 kg / h, and the bottom composition was 98.8% Pd metal ion liquid catalyst and 1.2% other components.

[0115] Comparative Example 1

[0116] Referring to the method of Example 1, the difference is that the reaction section and extraction section of the reactive extractive distillation column are changed to the same tray structure as the rectification section, with no other internal components. Other operations are the same as in Example 1. The DIB conversion rate is 85%, and the isononanal yield is 60%. Samples from the top and bottom of the reactive extractive distillation column are taken for analysis. The top flow rate is 1229 kg / h, and the top composition is: isononane 63.3%, DIB 35.6%, and other components 1.1%. The bottom flow rate is 3872 kg / h, and the bottom composition is: isononanal 57%, dimethyl terephthalate 38.7%, macromolecular condensate 2%, and catalyst 2.3%. The product purification column yields 2207 kg / h of isononanal at the top.

[0117] Comparative Example 2

[0118] Following the method of Example 1, the difference lies in that the reaction section of the reactive extractive distillation column is modified to have the same tray structure as the rectification section, with no other internal components. All other operations are the same as in Example 1. The DIB conversion rate is 92%, and the isononanal yield is 71%. Samples from the top and bottom of the reactive extractive distillation column are analyzed. The top flow rate is 881 kg / h, and the top composition is: isononane 71.9%, DIB 27.2%, and other components 0.9%. The bottom flow rate is 4290 kg / h, and the bottom composition is: isononanal 60.8%, dimethyl terephthalate 35%, macromolecular condensate 2.2%, and catalyst 2%. 2608.3 kg / h of isononanal is obtained from the top of the product purification column.

[0119] Comparative Example 3

[0120] Following the method of Example 1, the difference lies in that the extraction section of the reactive extractive distillation column is replaced with a tray structure identical to the rectification section, without any other internal components. All other operations are the same as in Example 1. The DIB conversion rate is 90%, and the isononanal yield is 76%. Samples from the top and bottom of the reactive extractive distillation column are analyzed. The top flow rate is 910.7 kg / h, and the composition is: isononane 66%, DIB 33%, and other components 1%. The bottom flow rate is 4480.7 kg / h, and the composition is: isononanal 62.4%, dimethyl terephthalate 33.5%, macromolecular condensate 2.1%, and catalyst 2%. The product purification column yields 2890 kg / h of isononanal at the top.

[0121] A comparison of Example 1 with Comparative Examples 1-3 reveals the following:

[0122] Under the same conditions, compared with Comparative Examples 1 to 3, Example 1 showed significantly improved reaction and extraction effects, with a significant increase in conversion rate, yield, and output. In Example 1, there was virtually no DIB at the top and bottom of the column, while in Comparative Examples 1 to 3, a large amount of DIB was present at the top of the reaction extractive distillation column. The DIB would be collected together with isononane, making it impossible to separate and resulting in DIB waste. However, there was no DIB waste in Example 1.

[0123] Although the present invention has been described in detail through the preferred embodiments described above, it should be understood that the above description should not be considered as a limitation of the present invention. Those skilled in the art will understand that modifications or adjustments can be made to the present invention based on the teachings of this specification. These modifications or adjustments should also be within the scope defined by the claims of the present invention.

Claims

1. A production apparatus for the hydroformylation of olefins to synthesize aldehydes, characterized in that, The production apparatus includes a reactive extractive distillation column, which consists of a stripping section, a reaction section, an extraction section, and a rectification section from bottom to top. The reaction section is a partitioned tower structure, with distillation separation on the left side of the partition and hydroformylation reaction on the right side of the partition; The extraction section is an eccentric rotating disk structure. An arc-shaped vertical partition divides the extraction section into left and right sides. The left side of the partition is the liquid phase clarification zone, and the eccentric rotating disk is on the right side of the partition, which is the gas-liquid mixing zone. An extractant inlet is provided on the left side of the partition at the top of the extraction section. The extractant can overflow into the right rotating disk and then return to the left side to perform multi-stage countercurrent extraction with the rising material at the bottom. The extracted phase flows from the left side of the bottom partition to the reaction section.

2. The production apparatus according to claim 1, characterized in that, A multi-layer tray is installed in the upper middle part of the right side of the partition, and the raw material inlet and syngas inlet are respectively located in the lower middle part and bottom of the right side of the partition, forming a plug flow bubbling reactor.

3. The production apparatus according to claim 1, characterized in that, It also includes a flash tank, a gas-liquid separator, a light component separation tower, and a product refining tower. The inlet of the flash tank is connected to the top outlet of the reactive extractive distillation tower, the top outlet of the flash tank is connected to the inlet of the gas-liquid separator, the bottom outlet of the flash tank is connected to the inlet of the light component separation tower, the top gas phase outlet of the gas-liquid separator is connected to the syngas inlet of the reactive extractive distillation tower, the bottom liquid phase outlet of the gas-liquid separator is connected to the inlet of the light component separation tower, the inlet of the product refining tower is connected to the bottom outlet of the reactive extractive distillation tower, and the side-stream outlet of the product refining tower is connected to the extractant inlet of the reactive extractive distillation tower.

4. The production apparatus according to claim 1, 2, or 3, characterized in that, The left side of the reaction section partition has a length a1 of 0.7-5.6m, with 5-10mm holes spaced at equal intervals; the right side of the partition has a length b1 of 0.3-2.4m, with 1-3mm holes spaced at equal intervals to prevent the reaction liquid from flowing out from the bottom of the reaction section; the partition height c1 is 0.8-2.4m; the distance d1 from the top of the partition to the catalyst feed line is 0.5-1.5m; the distance e1 from the catalyst feed inlet to the reactant feed inlet is 0.2-0.6m; the distance f1 from the reactant feed inlet to the bottom of the reaction section is 0.1-0.3m; the distance from the partition to the catalyst feed inlet is 0.2-2.4m; the right side of the partition has 4-8 trays, with 1-3mm holes spaced at equal intervals on the trays.

5. The production apparatus according to claim 4, characterized in that, The reaction section is an elliptical cylinder, and a liquid distributor is installed on the top left side of the reaction section partition.

6. The production apparatus according to claim 4, characterized in that, The partition in the extraction section has no holes on the left side and 1-3mm holes on the right side. The turntable speed is 60-100rpm. The length a2 of the left side of the partition is 0.2-2m. The length b2 of the right side of the partition is 0.8-6m. The spacing C2 between each partition in the extraction section is 0.2-0.6m.

7. A process for synthesizing aldehydes by hydroformylation of olefins, characterized in that, The production apparatus according to any one of claims 1 to 6 comprises the following steps: 1) The feed olefins enter the bubble reactor on the right side of the reaction section of the reaction extractive distillation column and are mixed with the catalyst. Syngas is then introduced to carry out the hydroformylation reaction under high pressure. 2) The olefin formylation product from step 1) overflows into the rectification section on the left side of the partition for separation. The light component evaporates to the extraction section, and the heavy component enters the stripping section. 3) The light components from step 2) containing alkane byproducts and olefin feedstocks with similar boiling points enter the extraction section of the reactive extractive distillation column for extraction and separation. 4) The light components separated from the extraction in step 3) enter the rectification section of the reactive extractive distillation column for further separation to obtain the light component feed stream at the top of the column, while the heavy components are returned to the extraction section for further extraction and separation; 5) The heavy components from step 2) enter the stripping section of the reactive extractive distillation column for separation, and the bottom of the column yields a heavy component feed stream containing aldehyde products.

8. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 7, characterized in that, The light component material obtained in step 4) is flashed under reduced pressure in a flash tank, where the vapor and liquid are initially separated. After the vapor phase is cooled, it is further separated in a gas-liquid separator. The separated vapor phase is pressurized by a circulating compressor and enters the bottom of the reactive extractive distillation column together with fresh syngas. The separated liquid phase enters the light component separation column for further separation.

9. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 8, characterized in that, In step 5), the recombinant feed stream of aldehyde-containing products obtained from the bottom of the tower passes through a scraper reboiler and then enters the product refining tower. The product refining tower is a partitioned tower. The aldehyde product is obtained at the top of the tower, the extractant is obtained in the upper side stream, the condensed recombinant component is obtained in the lower side stream, and the catalyst is obtained in the bottom of the tower.

10. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 8, characterized in that, Extractant and catalyst are discharged intermittently and replenished intermittently.

11. The process for synthesizing aldehydes by hydroformylation of olefins according to any one of claims 7-10, characterized in that, In step 1), the reaction raw materials are introduced from the lower right side of the partition and sprayed upwards, the catalyst is introduced from the middle and lower right side of the partition and sprayed downwards, and the synthesis gas enters through the small hole at the bottom right side of the partition.

12. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 11, characterized in that, The extract phase entering the reaction section continues to separate on the left side of the partition and in the stripping section. The light olefin component enters the reaction section to continue participating in the reaction, while the heavy component is discharged from the bottom of the column.

13. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 11, characterized in that, Syngas at room temperature enters from the bottom of the column, passes through the reaction section, and cools the reaction through throttling expansion and a large amount of circulating syngas, so that the reaction extractive distillation column maintains a good temperature gradient distribution.

14. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 11, characterized in that, The raw material olefin is one or more of C4-C12 isoolefins, or one or more of C4-C12 isoolefins and a small amount of alkanes.

15. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 14, characterized in that, The raw material olefins contain 80-95% C4-C12 isoolefins and 5-20% alkanes by mass.

16. The process for synthesizing aldehydes by hydroformylation of olefins according to any one of claims 7 to 10, characterized in that, The catalyst is a noble metal homogeneous ionic liquid catalyst.

17. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 16, characterized in that, The precious metal is selected from at least one of cobalt, rhodium, ruthenium, and palladium; the ligand is selected from any one of 2-(diphenylphosphine)pyridine, trifluoromethanesulfonic acid, methanesulfonic acid, toluenesulfonic acid, polysulfonic acid resin, butyl p-benzenesulfonate, and boric acid.

18. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 17, characterized in that, The noble metal is palladium; the ligand is butyl p-benzenesulfonate.

19. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 17, characterized in that, The molar ratio of catalyst, ligand and ionic liquid is 1:3:1 to 1:3:

3.

20. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 19, characterized in that, The molar ratio of catalyst, ligand, and ionic liquid is 1:3:

1.

21. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 16, characterized in that, The extractant is selected from one or more of the following: dimethyl terephthalate, meta-terephthalate, morpholine derivatives, sulfones, DMF, and C4-C16 nitrile.

22. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 21, characterized in that, The extractant is dimethyl terephthalate.

23. The process for synthesizing aldehydes by hydroformylation of olefins according to any one of claims 7 to 10, characterized in that, The theoretical plate number of the reactive extractive distillation column is 30-100; the diameter is 1-8m; the reflux ratio is 1-20; and the overall pressure drop is 0.2-10 bar.

24. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 23, characterized in that, The theoretical plate number of the reactive extractive distillation column is 60-70; the diameter is 1-4m; the reflux ratio is 5-10; and the overall pressure drop is 1-5bar.

25. The process for synthesizing aldehydes by hydroformylation of olefins according to any one of claims 7 to 10, characterized in that, The catalyst content in the reaction solution is 1%-6% by mass; the reaction temperature is 120-220℃; the reaction pressure is 1-150 barA; the reaction residence time is 0.5-3h; the pressure drop in the bubbling reactor is 0.1-2 bar; and the ratio of hydrogen to CO in the synthesis gas is 1:0.5-2.

26. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 25, characterized in that, The catalyst content in the reaction solution is 2%-4% by mass; the reaction temperature is 150-200℃; the reaction pressure is 10-50 barA; the reaction residence time is 1-2 h; the pressure drop of the bubbling reactor is 0.5-1.5 bar; and the ratio of hydrogen to CO in the synthesis gas is 1:1-1.

5.

27. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 8, characterized in that, The theoretical number of plates for the light component separation tower is 5-30; the reflux ratio is 0.5-10; the tower top pressure is 0.2-10 barA; and the overall tower pressure drop is 1-10 kPa.

28. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 27, characterized in that, The theoretical number of plates for the light component separation tower is 10-20; the reflux ratio is 5-10; the top pressure is 0.2-5 barA; and the overall pressure drop is 1-5 kPa.

29. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 9, characterized in that, The theoretical number of plates in the product refining column is 20-50; the reflux ratio is 0.5-5; the pressure at the top of the column is 1-10 kPaA; and the pressure drop across the entire column is 0.5-5 kPa.

30. The process for synthesizing aldehydes by hydroformylation of olefins according to claim 29, characterized in that, The theoretical number of plates in the product refining tower is 20-30; the reflux ratio is 0.5-2; the tower top pressure is 1-5 kPaA; and the overall tower pressure drop is 0.5-2 kPa.

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