Preparation system of butyraldehyde-butanol mixture

Abstract

The utility model provides a butyraldehyde-butanol mixture preparation system, which comprises a high-pressure reactor, a high-pressure reactor, a high-pressure reactor and a high-pressure reactor, wherein a partition plate is arranged in the middle of the high-pressure reactor; a first reaction zone is arranged above the partition plate, a second reaction zone is arranged below the partition plate, and catalyst inlets are formed in the side walls of the first reaction zone and the second reaction zone; a propylene inlet and a carbon monoxide inlet are formed in the side wall of the first reaction zone; a first bubble crushing unit is arranged in the first reaction area; a mixed gas inlet is formed in the side wall of the second reaction area; and a second bubble crushing unit is arranged in the second reaction area. The system disclosed by the utility model is simple in overall structure, and butyraldehyde-butanol is prepared by arranging the two reaction areas, so that the reaction efficiency is improved; meanwhile, the bubble crushing unit is arranged in the high-pressure reactor, so that the phase boundary mass transfer area of gas and liquid phases can be increased, the gas utilization rate and the reaction efficiency are improved, the energy consumption and the raw material loss are reduced, and the operation process is simplified.

Description

Technical Field

[0001] The utility model belongs to the technical field of butyraldehyde and butanol preparation, in particular to a butyraldehyde-butanol mixture preparation system. Background Art

[0002] In the chemical industry, butanol and butyraldehyde are extremely important chemicals, which are widely used in the manufacture of plastics, solvents and various chemical products. Butanol is usually obtained by hydrogenation reduction of butyraldehyde, while the production of butyraldehyde mainly depends on the hydroformylation reaction of propylene and carbon monoxide. In the prior art, the hydroformylation reaction process usually uses metal rhodium as a catalyst. Although a variety of rhodium-based catalysts have been developed, these methods face the problems of low conversion rate and complicated reaction steps. First, the butyraldehyde generated by the reaction needs to go through a complex separation process to obtain high-purity butyraldehyde, and then hydrogenation reduction can be carried out to produce butanol. This not only increases production costs, but also reduces overall production efficiency.

[0003] Moreover, the current butyraldehyde and butanol production process is limited by its multi-step operation, high energy consumption and complicated separation process. In particular, in the process of directly preparing butyraldehyde-butanol mixture from propylene and carbon monoxide, the existing technology cannot effectively simplify the production steps and the conversion of propylene and carbon monoxide gas during the reaction is incomplete, and the utilization rate of gas is low. In addition, the traditional method requires expensive catalysts and high-investment equipment, which further increases the production cost.

[0004] In view of this, the present utility model is proposed. Utility Model Content

[0005] The utility model aims to provide a system for preparing a butyraldehyde-butanol mixture. The system has a simple overall structure and improves reaction efficiency by setting two reaction zones for preparing butyraldehyde-butanol. Meanwhile, a bubble crushing unit is set in a high-pressure reactor to increase the mass transfer area of ​​the gas-liquid interface, improve gas utilization and reaction efficiency, reduce energy consumption and raw material loss, and simplify the operation process.

[0006] In order to achieve the above-mentioned purpose of the utility model, the following technical solutions are adopted:

[0007] The utility model provides a system for preparing a butyraldehyde-butanol mixture, comprising:

[0008] A high-pressure reactor, wherein a partition plate is disposed in the middle of the high-pressure reactor; a first reaction zone is disposed above the partition plate, and a second reaction zone is disposed below the partition plate, and catalyst inlets are disposed on the side walls of the first reaction zone and the second reaction zone;

[0009] The side wall of the first reaction zone is provided with a propylene inlet and a carbon monoxide inlet; the first reaction zone is provided with a first bubble breaking unit;

[0010] The side wall of the second reaction zone is provided with a mixed gas inlet; and the second bubble breaking unit is arranged in the second reaction zone.

[0011] In the prior art, the butyraldehyde generated by the reaction needs to go through a complicated separation process to obtain high-purity butyraldehyde, and then it can be hydrogenated and reduced to produce butanol. The current butyraldehyde and butanol production process is limited by its multi-step operation, high energy consumption and complicated separation process. In particular, in the process of directly preparing a butyraldehyde-butanol mixture from propylene and carbon monoxide, the existing technology cannot effectively simplify the production steps and the conversion of propylene and carbon monoxide gas during the reaction is incomplete, and the utilization rate of the gas is low.

[0012] The utility model simplifies the preparation process of a butyraldehyde-butanol mixture, does not require complex and cumbersome devices, and prepares the butyraldehyde-butanol mixture through a one-step method. In device selection, the utility model adopts a high-pressure reactor as a reaction device, and divides the high-pressure reactor into two reaction zones by arranging a partition plate, so as to realize the function of performing two-stage reactions in the same reaction zone, wherein the first reaction zone is a pre-reaction zone, which is used for performing hydroformylation of propylene and carbon monoxide to prepare butyraldehyde; the second reaction zone is a main reaction zone, which is used for further reacting the butyraldehyde that is not completely reacted and generated in the first reaction zone to generate a butyraldehyde-butanol mixture; and a first bubble crushing unit and a second bubble crushing unit are respectively arranged inside the first reaction zone and the second reaction zone, so as to crush and disperse the reaction raw materials in the reactor into micron-level bubbles, improve the solubility of the gas, and simultaneously increase the contact area between the gas-liquid two phases, thereby improving the utilization rate of the raw materials.

[0013] Preferably, the first bubble crushing unit includes a first bubble breaker arranged at the bottom of the first reaction zone and a plurality of diffusion disks arranged above the first bubble breaker, and there is an empty layer between two adjacent diffusion disks. By arranging the first bubble breaker, propylene and carbon monoxide gases can be crushed and dispersed. By arranging the diffusion disk above the first bubble breaker, the bubbles coming out of the first bubble breaker can be further refined by the combined use of the first bubble breaker and the diffusion disk, the surface area of ​​gas-liquid contact can be increased, and the material transfer efficiency can be improved; at the same time, the diffusion disk can make the gas-liquid distribution more uniform and reduce gas aggregation. By arranging the empty layer, the gas flow path is optimized, and the bubbles are prevented from excessively aggregating during the rising process, thereby maintaining the minimum size of the bubbles coming out of the first bubble breaker and the diffusion disk, and further improving the efficiency of the gas-liquid reaction and the gas utilization rate.

[0014] Preferably, a plurality of crossbeams for supporting the diffusion disks are connected between adjacent diffusion disks, and the plurality of crossbeams divide the empty layer into a plurality of independent areas. By dividing the empty layer into a plurality of independent areas by the crossbeams, the path of the gas from the first bubble breaker through the diffusion disk can be effectively controlled, thereby making the gas evenly distributed, increasing the chance of gas-liquid contact, and enhancing the uniformity and efficiency of the reaction. By optimizing the distribution and mass transfer process of the gas, the efficiency of the reaction is improved, and the yield of butyraldehyde and butanol is increased. At the same time, the supporting effect of the crossbeams can enhance the overall structural stability of the diffusion disk.

[0015] Preferably, the second bubble breaker unit includes a second bubble breaker and a third bubble breaker, the second bubble breaker is arranged above the third bubble breaker and the second bubble breaker and the third bubble breaker are arranged in the same straight line, a connecting pipe is arranged between the second bubble breaker and the third bubble breaker, and an output hole for outputting internal materials is arranged in the middle of the connecting pipe. By arranging two bubble breakers and arranging them in the up-down direction, the raw materials coming out of the two bubble breakers can be hedged, the bubble size can be further refined, the surface area of ​​gas-liquid contact can be increased, and the reaction uniformity can be improved, thereby improving the reaction speed and efficiency.

[0016] Moreover, the second reaction zone of the utility model serves as the main reaction zone, and needs to further hydrogenate the butyraldehyde and its unreacted raw materials overflowing from the first reaction zone to generate a butyraldehyde-butanol mixture. Therefore, the second bubble crushing unit not only needs to continue to provide good bubble crushing and dispersion effects, but also needs to consider the effective dispersion and utilization of the hydrogenation gas to ensure the full reaction of butyraldehyde. The utility model arranges two relatively arranged bubble breakers in the second bubble crushing unit, which can produce smaller and more evenly distributed bubbles, reduce the occurrence of local over-reaction or unreacted areas, and improve product quality.

[0017] Preferably, a plurality of throttling discs are arranged inside the connecting pipe, and the distance between two adjacent throttling discs is equal. By arranging the throttling discs in the connecting pipe, the local pressure drop generated by the throttling discs in the connecting pipe increases the shear force of the fluid, which can further refine the bubbles passing through, so that the bubbles reach a smaller size before entering the second reaction zone, thereby increasing the surface area of ​​gas-liquid contact and improving the solubility of the gas. At the same time, by evenly arranging the throttling discs, the gas will experience a pressure drop and speed adjustment when flowing through each layer of throttling discs, which can extend the reaction time on the one hand, and make the gas distribution more uniform on the other hand, which is conducive to improving the reaction efficiency of the entire reaction system and the conversion rate of the reactants.

[0018] Preferably, a stirring assembly is provided below the second bubble crushing unit, and the stirring assembly includes a stirring shaft and a stirring blade installed at the end of the stirring shaft. When the tiny bubbles generated by the second bubble crushing unit pass through the stirring zone, the movement of the stirring blade further disperses the bubbles, increases the gas-liquid contact area, and thus improves the gas dissolution rate and mass transfer efficiency. The stirring assembly ensures the continuous flow of the entire reaction liquid, so that the reactants in the reaction zone can be continuously updated, ensuring the uniformity of the reaction.

[0019] Those skilled in the art can understand that the bubble breaker used in the present invention has been embodied in the prior patents of the present invention, such as patents with application numbers CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660, CN105903425A, CN109437390A, CN205833127U and CN207581700U. The prior patent CN201610641119.6 describes in detail the specific product structure and working principle of the micron bubble generator (i.e., bubble breaker). The application document states that "the micron bubble generator includes a main body and a secondary crushing member, a cavity is provided in the main body, an inlet connected to the cavity is provided on the main body, the first and second opposite ends of the cavity are open, wherein the cross-sectional area of ​​the cavity decreases from the middle of the cavity to the first and second ends of the cavity; the secondary crushing member is provided at at least one of the first and second ends of the cavity, a part of the secondary crushing member is provided in the cavity, and an annular channel is formed between the secondary crushing member and the through holes open at both ends of the cavity. The micron bubble generator also includes an air inlet pipe and a liquid inlet pipe." From the specific structure disclosed in the application document, it can be known that its specific working principle is: the liquid enters the micron bubble generator tangentially through the liquid inlet pipe, rotates at ultra-high speed and cuts the gas, so that the gas bubbles are broken into micron-level microbubbles, thereby increasing the mass transfer area between the liquid phase and the gas phase, and the micron bubble generator in the patent is a pneumatic bubble breaker.

[0020] In addition, the prior patent 201610641251.7 records that the primary bubble breaker has a circulating liquid inlet, a circulating gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker connects the feed port with the gas-liquid mixture outlet, indicating that the bubble breaker requires gas-liquid mixture to enter. In addition, it can be seen from the following figures that the primary bubble breaker mainly uses circulating liquid as power, so the primary bubble breaker actually belongs to a hydraulic enhanced reactor, and the secondary bubble breaker simultaneously passes the gas-liquid mixture into an elliptical rotating ball for rotation, thereby achieving bubble breaking during the rotation process, so the secondary bubble breaker actually belongs to a gas-liquid linkage type bubble breaker. In fact, whether it is a hydraulic bubble breaker or a gas-liquid linkage type bubble breaker, it is a specific form of a bubble breaker. However, the bubble breaker adopted by the utility model is not limited to the above-mentioned forms. The specific structure of the bubble breaker recorded in the prior patent is only one of the forms that can be adopted by the utility model.

[0021] In addition, the prior patent 201710766435.0 records that "the principle of the bubble breaker is a high-speed jet to achieve mutual collision of gases"; and the prior patent CN106187660 also has relevant records on the specific structure of the bubble breaker, see paragraphs

[0031] -

[0041] in the specification, and the drawings, which explain in detail the specific working principle of the bubble breaker S-2. The top of the bubble breaker is a liquid phase inlet, and the side is a gas phase inlet. The liquid phase coming in from the top provides suction power, thereby achieving the effect of crushing into ultrafine bubbles. It can also be seen in the drawings that the bubble breaker has a conical structure, and the diameter of the upper part is larger than the diameter of the lower part, so that the liquid phase can better provide suction power.

[0022] Since the bubble breaker was just developed in the early stage of the prior patent application, it was named micron bubble generator (CN201610641119.6) in the early stage. With the continuous technical improvement, it was renamed as bubble breaker in the later stage. Now the bubble breaker in the utility model is equivalent to the previous micron bubble generator, micro interface generator, etc., but the name is different. In summary, the bubble breaker of the utility model belongs to the prior art.

[0023] Preferably, an overflow pipe is provided in the first reaction zone, and the overflow pipe penetrates the partition plate to connect the first reaction zone and the second reaction zone; the product generated in the first reaction zone enters the second reaction zone through the overflow pipe. The overflow pipe allows the raw materials and intermediate products that are not completely reacted in the first reaction zone to directly enter the second reaction zone for further reaction, thereby reducing the waste of raw materials and improving the utilization rate of raw materials.

[0024] Preferably, a gas collecting chamber is provided at the top of the first reaction zone, the gas collecting chamber is higher than the liquid level in the first reaction zone, and the gas outlet of the gas collecting chamber is connected to the first crushing unit to recover the unreacted gas in the first reaction zone. The unreacted gas can be recovered by providing the gas collecting chamber, and the gas collecting chamber can effectively collect the unreacted or partially reacted gas raw materials (such as propylene and carbon monoxide) in the first reaction zone, and re-introduce them into the first bubble crushing unit through the gas outlet for reuse. Such a recycling process reduces the loss of raw materials, improves the utilization efficiency of raw materials and reduces environmental pollution.

[0025] Preferably, a defoaming tray is provided below the gas collecting chamber, the defoaming tray is located above the first bubble crushing unit and the defoaming tray is provided below the liquid surface of the first reaction zone. By providing the defoaming tray, large bubbles generated by the reaction can be destroyed, thereby improving the recovery efficiency of the gas.

[0026] Preferably, the preparation system of the butyraldehyde-butanol mixture further comprises:

[0027] A propylene storage tank, a carbon monoxide storage tank and a hydrogen storage tank, wherein the propylene storage tank and the carbon monoxide storage tank are respectively connected to the propylene inlet and the carbon monoxide inlet on the side wall of the first reaction zone; the hydrogen storage tank and the carbon monoxide storage tank are connected to the mixed gas inlet on the side wall of the second reaction zone after being mixed in a mixed gas storage tank;

[0028] A gas-liquid separator, the gas-liquid separator is connected to the outlet at the bottom end of the high-pressure reactor;

[0029] A condenser is connected to the bottom end of the gas-liquid separator.

[0030] Preferably, the outlet of the condenser is connected to a mixed liquid separator for separating butyraldehyde and butanol.

[0031] Compared with the prior art, the beneficial effects of the utility model are:

[0032] (1) By setting a partition plate in the high-pressure reactor, a graded reaction is achieved. At the same time, by cooperating with a bubble crushing unit, the solubility of the gas and the contact area between the gas and liquid phases are increased, thereby improving the reaction efficiency and the conversion rate of the raw materials.

[0033] (2) By arranging a connecting pipe and a throttling disk in the second bubble crushing unit, a local pressure drop can be generated in the connecting pipe, which increases the shear force of the fluid and can further refine the bubbles passing through, so that the bubbles reach a smaller size before entering the second reaction zone, thereby increasing the surface area of ​​gas-liquid contact and improving the solubility of the gas.

[0034] (3) By setting up an overflow pipe to achieve continuous material transfer between the first reaction zone and the second reaction zone, as well as the design of the gas collecting chamber and the defoaming plate, the system can more effectively control the reaction conditions, reduce the loss of unreacted gas, and prevent excessive generation of reactant foam. BRIEF DESCRIPTION OF THE DRAWINGS

[0035] By reading the detailed description of the preferred embodiment below, various other advantages and benefits will become clear to those of ordinary skill in the art. The accompanying drawings are only used for the purpose of illustrating the preferred embodiment and are not considered to be limiting of the present invention. Moreover, the same reference symbols are used throughout the accompanying drawings to represent the same components. In the accompanying drawings:

[0036] Figure 1 A schematic flow chart of a system for preparing a butyraldehyde-butanol mixture provided in Example 1 of the present invention.

[0037] in:

[0038] 1-high pressure reactor; 101-catalyst inlet;

[0039] 2-separator plate; 3-first reaction zone;

[0040] 301-propylene inlet; 302-carbon monoxide inlet;

[0041] 303-gas collecting chamber; 304-foam removal tray;

[0042] 4-second reaction zone; 401-mixed gas inlet;

[0043] 402-stirring assembly; 4021-stirring shaft;

[0044] 4022-stirring fan blade; 5-overflow pipe;

[0045] 6-first bubble breaker unit; 601-first bubble breaker;

[0046] 602-diffusion disk; 603-empty layer;

[0047] 604- beam; 7- second bubble crushing unit;

[0048] 701-second bubble breaker; 702-third bubble breaker;

[0049] 703-connecting pipe; 704-throttling disc;

[0050] 8-propylene storage tank; 9-carbon monoxide storage tank;

[0051] 10-Hydrogen storage tank; 11-Gas-liquid separator;

[0052] 12-condenser; 13-mixed gas storage tank;

[0053] 14-Mixed liquid separator. DETAILED DESCRIPTION

[0054] The technical solution of the utility model will be clearly and completely described below in conjunction with the accompanying drawings and specific embodiments, but those skilled in the art will understand that the embodiments described below are part of the embodiments of the utility model, rather than all of the embodiments, and are only used to illustrate the utility model, and should not be considered as limiting the scope of the utility model. Based on the embodiments in the utility model, all other embodiments obtained by ordinary technicians in the field without making creative work are within the scope of protection of the utility model. If the specific conditions are not specified in the embodiments, they are carried out according to conventional conditions or conditions recommended by the manufacturer. If the manufacturer is not specified for the reagents or instruments used, they are all conventional products that can be purchased commercially.

[0055] In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, the terms "first", "second", and "third" are used for descriptive purposes only, and cannot be understood as indicating or implying relative importance.

[0056] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installation", "connection" and "connection" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0057] In order to more clearly explain the technical solution of the present invention, it is described in the form of specific embodiments below.

[0058] Example 1

[0059] See also Figure 1As shown, a system for preparing a butyraldehyde-butanol mixture according to an embodiment of the utility model comprises a high-pressure reactor 1, wherein a partition plate 2 is arranged in the middle of the high-pressure reactor 1, and the partition plate 2 divides the upper part of the high-pressure reactor 1 into a first reaction zone 3, and divides the lower part of the high-pressure reactor 1 into a second reaction zone 4. The side walls of the first reaction zone 3 and the second reaction zone are provided with a catalyst inlet 101.

[0060] Preferably, an overflow pipe 5 is provided in the first reaction zone 3 , and the overflow pipe 5 penetrates the partition plate 2 to connect the first reaction zone 3 and the second reaction zone 4 , and the product generated in the first reaction zone 3 enters the second reaction zone 4 through the overflow pipe 5 .

[0061] Preferably, a propylene inlet 301 and a carbon monoxide inlet 302 are provided on the side wall of the first reaction zone 3; and a first bubble crushing unit 6 is provided in the first reaction zone 3; wherein the first bubble crushing unit 6 comprises a first bubble breaker 601 provided at the bottom of the first reaction zone 3 and a plurality of diffusion disks 602 provided above the first bubble breaker 601, and an empty layer 603 exists between two adjacent diffusion disks 602; specifically, a plurality of beams 604 for supporting the diffusion disks 602 are connected between adjacent diffusion disks 602, and the plurality of beams 604 divide the empty layer 603 into a plurality of independent areas.

[0062] A gas collecting chamber 303 is provided on the top of the first reaction zone 3 , and the gas collecting chamber 303 is higher than the liquid level in the first reaction zone 3 . The gas outlet of the gas collecting chamber 303 is connected to the first crushing unit to recover the unreacted gas in the first reaction zone 3 .

[0063] Preferably, a defoaming tray 304 is provided below the gas collecting chamber 303 , and the defoaming tray 304 is located above the first bubble breaking unit 6 and below the liquid surface of the first reaction zone 3 .

[0064] Preferably, the side wall of the second reaction zone 4 is provided with a mixed gas inlet 401; and a second bubble crushing unit 7 is provided in the second reaction zone 4. The second bubble crushing unit 7 comprises a second bubble breaker 701 and a third bubble breaker 702, the second bubble breaker 701 is arranged above the third bubble breaker 702 and the second bubble breaker 701 and the third bubble breaker 702 are arranged in the same straight line, and a connecting pipe 703 is provided between the second bubble breaker 701 and the third bubble breaker 702. A multi-layer throttling disc 704 is provided inside the connecting pipe 703, and the distance between two adjacent throttling discs 704 is equal.

[0065] Preferably, a stirring assembly 402 is provided below the second bubble crushing unit 7 , and the stirring assembly 402 includes a stirring shaft 4021 and a stirring blade 4022 installed at the end of the stirring shaft 4021 .

[0066] The preparation system of the butyraldehyde-butanol mixture of the present embodiment also includes:

[0067] A propylene storage tank 8, a carbon monoxide storage tank 9 and a hydrogen storage tank 10, wherein the propylene storage tank 8 and the carbon monoxide storage tank 9 are respectively connected to the propylene inlet 301 and the carbon monoxide inlet 302 on the side wall of the first reaction zone 3, and the hydrogen storage tank 10 and the carbon monoxide storage tank 9 are mixed through the mixed gas storage tank 13 and connected to the mixed gas inlet 401 on the side wall of the second reaction zone 4.

[0068] The gas-liquid separator 11 is connected to the outlet at the bottom end of the high-pressure reactor 1 .

[0069] The condenser 12 is connected to the bottom end of the gas-liquid separator 11 .

[0070] The mixed liquid separator 14 is connected to the outlet of the condenser 12 .

[0071] Example 2

[0072] The difference between Example 2 and Example 1 is that the first bubble breaker is arranged in the upper part of the first reaction zone.

[0073] Example 3

[0074] The only difference between Example 3 and Example 1 is that the second bubble breaker and the third bubble breaker are not arranged on the same straight line.

[0075] Comparative Example 1

[0076] The difference between Comparative Example 1 and Example 1 is that the first bubble crushing unit is not provided.

[0077] Comparative Example 2

[0078] The difference between Comparative Example 2 and Example 1 is that the second bubble crushing unit is not provided.

[0079] Comparative Example 3

[0080] The difference between Comparative Example 3 and Example 1 is only that the first bubble breaker is not provided.

[0081] Comparative Example 4

[0082] The difference between Comparative Example 4 and Example 1 is that no diffusion disk is provided.

[0083] Comparative Example 5

[0084] The difference between Comparative Example 5 and Example 1 is only that no communicating pipe is provided.

[0085] Comparative Example 6

[0086] The only difference between Comparative Example 6 and Example 1 is that no throttling disk is provided inside the communicating pipe.

[0087] Comparative Example 7

[0088] Comparative Example 7 uses relevant technology to prepare a butyraldehyde-butanol mixture.

[0089] Experimental Example 1

[0090] The reaction systems of Examples 1-3 and Comparative Examples 1-7 were used to prepare the butyraldehyde-butanol mixture. The specific experimental conditions were as follows: triphenylphosphine-ruthenium, triphenylphosphine-rhodium, and toluene were selected as catalysts, wherein the mass ratio of triphenylphosphine-rhodium to triphenylphosphine-ruthenium was 10:100, and the reaction results were shown in Table 1 below.

[0091] Propylene conversion rate (%) Butanol ratio (%) Butyraldehyde ratio (%) Example 1 99.9 94 5 Example 2 98.2 92 6 Example 3 96.6 88 7 Comparative Example 1 91.6 83 7 Comparative Example 2 94.5 82 9 Comparative Example 3 93.3 84 8 Comparative Example 4 89.9 75 12 Comparative Example 5 88.3 72 15 Comparative Example 6 86.6 70 16 Comparative Example 7 80.5 60 20

[0092] Combined with the experimental data of Experimental Example 1, it can be obtained that when preparing butyraldehyde-butanol in the prior art, the conversion rate of propylene is about 80%, of which the proportion of butanol is about 60% and the proportion of butyraldehyde is about 20%. Combined with Tables 1-3 above, it can be seen that compared with the prior art, the propylene conversion rate in each embodiment of the utility model is significantly improved, and in the product, the proportion of butanol and the proportion of butyraldehyde are also significantly higher than the prior art, and the propylene conversion rate of Example 1 reaches 99.9%.

[0093] Moreover, Example 1 of the utility model is the best example, because the reaction system of Example 1 uses the bubble crushing unit in conjunction with the high-pressure reactor, and makes a different design for the key points of different reactions in the first reaction zone and the second reaction zone, and the proportion of butanol in the obtained product is significantly higher than that of the prior art and other examples and comparative examples, because the conversion rate of butanol is improved through the unique system design of Example 1 of the utility model. It is shown that the design method of Example 1 can achieve the best reaction effect, and it can be seen that the preparation system of Example 1 has a high raw material conversion rate and a good preparation effect.

[0094] Among them, the propylene conversion rate of Comparative Example 1 is lower than that of Example 1. This is because Comparative Example 1 does not have a first bubble crushing unit, which cannot fully crush and disperse the reaction raw materials in the first reaction zone, resulting in a low propylene conversion rate, and then resulting in a low proportion of overall butanol and butyraldehyde.

[0095] The propylene conversion rate and the proportion of butanol in the product of Comparative Example 2 are also significantly lower than those of Example 1. This is because Comparative Example 2 does not have a second bubble crushing unit, which cannot fully crush and disperse the raw materials and hydrogen in the second reaction zone, resulting in a low butyraldehyde conversion rate and a low proportion of butanol in the reaction products.

[0096] Finally, it should be noted that the above embodiments are only used to illustrate the technical solution of the utility model, rather than to limit it. Although the utility model has been described in detail with reference to the aforementioned embodiments, ordinary technicians in this field should understand that they can still modify the technical solutions recorded in the aforementioned embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not make the essence of the corresponding technical solution deviate from the scope of the technical solution of the embodiments of the utility model.

Claims

1. A system for preparing a butyraldehyde-butanol mixture, characterized in that: include: A high-pressure reactor, wherein a partition plate is disposed in the middle of the high-pressure reactor; a first reaction zone is disposed above the partition plate, and a second reaction zone is disposed below the partition plate, and catalyst inlets are disposed on the side walls of the first reaction zone and the second reaction zone; The side wall of the first reaction zone is provided with a propylene inlet and a carbon monoxide inlet; the first reaction zone is provided with a first bubble breaking unit; The side wall of the second reaction zone is provided with a mixed gas inlet; and the second bubble breaking unit is arranged in the second reaction zone.

2. The system for preparing a butyraldehyde-butanol mixture according to claim 1, characterized in that: The first bubble breaker unit includes a first bubble breaker arranged at the bottom of the first reaction zone and a plurality of diffusion disks arranged above the first bubble breaker, and an empty layer exists between two adjacent diffusion disks.

3. The system for preparing a butyraldehyde-butanol mixture according to claim 2, characterized in that: A plurality of cross beams for supporting the diffusion disks are connected between adjacent diffusion disks, and the plurality of cross beams divide the empty layer into a plurality of independent areas.

4. The system for preparing a butyraldehyde-butanol mixture according to claim 1, characterized in that: The second bubble breaker unit includes a second bubble breaker and a third bubble breaker, the second bubble breaker is arranged above the third bubble breaker and the second bubble breaker and the third bubble breaker are arranged in the same straight line, a connecting pipe is arranged between the second bubble breaker and the third bubble breaker, and an output hole for outputting internal materials is arranged in the middle of the connecting pipe.

5. The system for preparing a butyraldehyde-butanol mixture according to claim 4, characterized in that: Multiple layers of throttling discs are arranged inside the communicating pipe, and the distance between two adjacent throttling discs is equal.

6. The system for preparing a butyraldehyde-butanol mixture according to claim 1, characterized in that: A stirring assembly is arranged below the second bubble crushing unit, and the stirring assembly includes a stirring shaft and a stirring fan blade installed at the end of the stirring shaft.

7. The system for preparing a butyraldehyde-butanol mixture according to claim 1, characterized in that: An overflow pipe is arranged in the first reaction zone, and the overflow pipe penetrates the partition plate to connect the first reaction zone and the second reaction zone; the product generated in the first reaction zone enters the second reaction zone through the overflow pipe.

8. The system for preparing a butyraldehyde-butanol mixture according to claim 1, characterized in that: A gas collecting chamber is arranged on the top of the first reaction zone, and the gas collecting chamber is higher than the liquid level in the first reaction zone. The gas outlet of the gas collecting chamber is connected to the first bubble crushing unit to recover the unreacted gas in the first reaction zone.

9. The system for preparing a butyraldehyde-butanol mixture according to claim 8, characterized in that: A defoaming tray is disposed below the gas collecting chamber. The defoaming tray is located above the first bubble breaking unit and is disposed below the liquid surface of the first reaction zone.

10. The system for preparing a butyraldehyde-butanol mixture according to claim 1, characterized in that: The preparation system of the butyraldehyde-butanol mixture also includes: A propylene storage tank, a carbon monoxide storage tank and a hydrogen storage tank, wherein the propylene storage tank and the carbon monoxide storage tank are respectively connected to the propylene inlet and the carbon monoxide inlet on the side wall of the first reaction zone; the hydrogen storage tank and the carbon monoxide storage tank are connected to the mixed gas inlet on the side wall of the second reaction zone after being mixed in a mixed gas storage tank; A gas-liquid separator, the gas-liquid separator is connected to the outlet at the bottom end of the high-pressure reactor; A condenser is connected to the bottom end of the gas-liquid separator.

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