Production method of isononyl alcohol and production device of isononyl alcohol

Abstract

The invention belongs to the field of petrochemical industry, and relates to a production method of isononyl alcohol and a production device of isononyl alcohol. The production method of the isononyl alcohol comprises the following steps: C8 olefin, synthesis gas and a catalyst enter a raw material reactor to react to obtain a hydroformylation reaction product, the hydroformylation reaction product enters a product separation unit to separate and remove by-products, and then the hydroformylation reaction product enters an aldehyde hydrogenation unit to react to obtain the isononyl alcohol. The invention has the following beneficial effects: the product separation unit removes most of non-condensable steam, light components and water through a low-vacuum flash evaporation-high-vacuum evaporation two-stage process, reduces the load of a high-vacuum system, and saves energy consumption; the circulation path of the catalyst is shortened through the efficient and rapid separation process of the catalyst, and decomposition of the catalyst is reduced; by applying the vacuum evaporator, low-pressure and low-temperature rapid separation of materials is achieved, the catalyst circulation process is short, the separation temperature is low, and meanwhile energy consumption is saved.

Description

Technical Field

[0001] The invention belongs to the field of petrochemical industry, and in particular relates to a production method of isononyl alcohol and a production device of isononyl alcohol. Background Art

[0002] Olefins react with synthesis gas (CO+H2) under the action of transition metal cobalt or rhodium to generate aldehyde compounds with one more carbon atom than olefins. This reaction process is the hydroformylation reaction of olefins, which is the most successful and widely used homogeneous catalytic reaction process in industrial application. The generated aldehydes can be further processed into compounds such as alcohols, esters, ethers, carboxylic acids and amines.

[0003] Isononanol is divided into high-branched isononanol and low-branched isononanol according to the number of branches. Low-branched isononanol is used to produce plasticizers such as diisononyl phthalate (DINP), diisononyl adipate (DINA) and trihydroxymethyl triisononanoate (TINTM). These plasticizers have excellent performance and are non-toxic. They are mainly used in polyvinyl chloride, vinyl chloride copolymers, cellulose acetate, ethyl cellulose and synthetic rubber to replace dioctyl phthalate (DOP). DOP is potentially carcinogenic and has been banned or restricted in Europe and the United States. High-branched isononanol (3,5,5-trimethyl-1-hexanol) is a cosmetic additive. Isononanol uses C8 olefins and synthesis gas as reactants to generate C9 alcohol and C9 aldehyde under a certain temperature, pressure, and homogeneous catalysis of transition metal (Co or Ru) complexes. Side reactions include direct hydrogenation of reactant olefins and aldol condensation to generate heavy substances.

[0004] At present, the relevant technologies for the production of isononanol are as follows: (1) BASF process: It is divided into two stages, hydroformylation and hydrogenation. Hydroformylation uses low-branched olefins of carbon eight dimerized after etherification as raw materials, the reaction temperature is 190-210°C, the pressure is 25-30MPa, isononanal is generated and converted into low-branched isononanol through a subsequent hydrogenation process. (2) Exxon Mobil process: Low-branched octene is used as raw material and reacts with synthesis gas in a carbonylation reactor, the reaction temperature is 170-210°C, the pressure is 28-33MPa, the product is mainly aldehyde, and the crude aldehyde is hydrogenated to obtain the product. (3) Shell process: Generally, straight-chain olefins are used as raw materials, the reaction temperature is 190-220°C, the pressure is 7-10MPa, the product is mainly straight-chain alcohol, the aldehyde content is low, and hydrogenation is still required to convert the aldehyde into alcohol. (4) Low-pressure oxo synthesis LP OXO technology jointly owned by Johnson Matthey of the United Kingdom and Dow of the United States: In the early 21st century, Davy and Johnson Matthey developed the Johnson Matthey oxo alcohol process, the predecessor of which was the ICI high-pressure oxo alcohol process. The Johnson Matthey oxo alcohol process is suitable for the production of C7-C15 high-carbon oxo alcohols, especially for the production of isononyl alcohol and isodecanol using isooctene and isononylene as raw materials.

[0005] In summary, as an important chemical, isononanol has broad and important application scenarios. However, the traditional product separation process requires separating low-boiling point substances first and then high-boiling point substances according to boiling point. Due to the high boiling point of the catalyst, the catalyst is separated last, and there is a problem of large thermal decomposition of the catalyst. Summary of the invention

[0006] In order to solve the above problems existing in the prior art, the present invention provides a method for producing isononyl alcohol and a device for producing isononyl alcohol, which remove most of the non-condensable steam, light components and water through a two-stage process of low vacuum flash evaporation-high vacuum evaporation, reduce the load of the high vacuum system, and save energy consumption; and shorten the circulation path of the catalyst through a high-efficiency and rapid catalyst separation process, which is conducive to reducing the decomposition of the catalyst.

[0007] In order to achieve the above object, the first aspect of the present invention provides a method for producing isononyl alcohol, comprising the following steps:

[0008] C8 olefins, synthesis gas and catalyst enter the raw material reactor for reaction to obtain a hydroformylation reaction product, the hydroformylation reaction product enters the product separation unit for separation and removal of by-products, and then enters the aldehyde hydrogenation unit for reaction to obtain isononanol;

[0009] The step of the hydroformylation reaction product entering the product separation unit to separate and remove by-products comprises:

[0010] The hydroformylation reaction product enters a hot high-pressure separation tank for gas-liquid separation to obtain high-fraction gas and hot high-pressure separation tank bottom liquid, the high-fraction gas enters a circulating synthesis gas booster inlet separator tank for gas-liquid separation to obtain synthesis gas and circulating synthesis gas booster inlet separator tank bottom liquid; the hot high-pressure separation tank bottom liquid and the circulating synthesis gas booster inlet separator tank bottom liquid both enter a hot low-pressure separation tank for gas-liquid separation to obtain hot low-pressure separation tank bottom liquid and hot low-pressure separation tank top gas, the hot low-pressure separation tank top gas enters a low-fraction gas cooler for cooling to obtain fuel gas, the hot low-pressure separation tank bottom liquid enters a vacuum flash tank for gas-liquid separation to obtain vacuum flash tank bottom liquid and vacuum flash tank top gas, the vacuum flash tank top gas enters a flash tank top condenser for condensation to obtain light components to the flare C9 alcohol separation tower bottom liquid, the vacuum flash tank bottom liquid obtained is sent to a vacuum evaporator for gas-liquid separation to obtain catalyst-containing C9 alcohol and vacuum evaporator top gas;

[0011] The catalyst-containing C9 alcohol is divided into two parts, one part of which enters the heavy oil stripping tower for gas-liquid separation to obtain heavy oil and heavy oil stripping tower top gas, and the vacuum evaporator top gas enters the evaporator freezer for condensation to obtain evaporator top liquid;

[0012] The top gas of the heavy oil stripping tower and the top liquid of the evaporator are mixed and then enter the C9 alcohol separation tower for separation to obtain C8 gasoline and C9 alcohol separation tower bottom liquid, and the C9 alcohol separation tower bottom liquid is sent to the aldehyde hydrogenation unit.

[0013] The method of the present invention uses C8 olefins and synthesis gas as raw materials, and produces the important chemical isononyl alcohol through a raw material reactor, a product separation unit and an aldehyde hydrogenation unit. Through a two-stage process of low vacuum flash evaporation-high vacuum evaporation, most of the non-condensable steam, light components and water are removed, the load of the high vacuum system is reduced, and energy consumption is saved. The circulation path of the catalyst is shortened by the efficient and rapid separation process of the catalyst, which is conducive to reducing the decomposition of the catalyst. By using a vacuum evaporator, the material is quickly separated at low pressure and low temperature, the catalyst circulation process is short, the separation temperature is low, and energy consumption is saved.

[0014] In the present invention, the reaction is a homogeneous reaction, the catalyst is dissolved in the liquid, and the catalyst is easily deactivated at high temperature without the protection of synthesis gas. It is necessary to separate the catalyst as efficiently as possible and reduce the residence time in the evaporator to reduce catalyst decomposition.

[0015] In the present invention, a vacuum evaporator is used to achieve low-pressure and low-temperature rapid evaporation of a catalyst-containing liquid. The liquid in the evaporator is in a thin film shape, the evaporation heat transfer coefficient is large, the pressure drop is low, and the residence time is short, which will not cause the catalyst to degrade. The C9 alcohol containing the catalyst is first separated from the vacuum evaporator and recycled back to the reaction system, which shortens the circulation path of the catalyst and is beneficial to reducing the decomposition of the catalyst.

[0016] According to the present invention, preferably, the C8 olefin enters the C8 olefin feed buffer tank for buffering, then enters the raw material heater for heating, and then enters the raw material reactor.

[0017] Preferably, after the catalyst enters the catalyst preparation tank for preparation, it is mixed with another portion of C9 alcohol containing the catalyst, and then enters the circulating C9 alcohol buffer tank, and then enters the raw material reactor.

[0018] Preferably, after the synthesis gas enters the inlet separator tank of the supplementary synthesis gas compressor for pressurization, it is mixed with the synthesis gas at the top of the inlet separator tank of the circulating synthesis gas compressor and the C9 alcohol containing catalyst at the outlet of the circulating C9 alcohol buffer tank, and then passes through the product / circulating C9 alcohol heat exchanger to exchange heat with the liquid at the bottom of the hot high-pressure separation tank, enters the catalyst activation reactor for activation, and finally is mixed with the C8 olefins heated by the feedstock heater and enters the feedstock reactor.

[0019] According to the present invention, preferably, the operating temperature of the hot high-pressure separation tank is 160-200° C., and the operating pressure is 7-10 MPag(g).

[0020] According to the present invention, preferably, the operating temperature of the top of the hot low-pressure separation tank is 30-60°C, the operating temperature of the bottom of the tank is 110-130°C, and the operating pressure is 0.2-1.5 MPag(g).

[0021] According to the present invention, preferably, the operating temperature of the vacuum flash tank top is 0-20°C, the operating temperature of the tank bottom is 80-110°C, and the operating pressure is -0.1-0.1 MPag(g).

[0022] According to a specific embodiment of the present invention, the flash tank top condenser is cooled to 10° C. using a low-temperature refrigerant to condense the material as much as possible, reduce the vacuum system load and recover the product.

[0023] According to the present invention, preferably, the operating temperature of the vacuum evaporator is 90 to 120° C., and the operating pressure is -0.2 to 0.1 MPag(g).

[0024] According to the present invention, preferably, the operating temperature of the top of the heavy oil stripping tower is 180-210° C., the operating temperature of the bottom of the tower is 220-240° C., and the operating pressure is 0-0.1 MPag(g).

[0025] According to the present invention, preferably, the operating temperature of the top of the C9 alcohol separation tower is 90-120° C., the operating temperature of the bottom of the tower is 190-220° C., and the operating pressure is 0-0.2 MPag(g).

[0026] According to the present invention, preferably, the C8 olefin, synthesis gas and catalyst enter 3 to 8 hydroformylation reactors for reaction.

[0027] Preferably, the reaction temperature of each hydroformylation reactor is 160-200° C.; and the reaction pressure is 7-10 MPag(g).

[0028] A second aspect of the present invention provides a production device for isononanol, the production device comprising: a catalyst feed pipeline, a C8 olefin feed pipeline, a synthesis gas feed pipeline, a raw material reactor, a product separation unit and an aldehyde hydrogenation unit;

[0029] The product separation unit includes: a hot high-pressure separation tank, a circulating synthesis gas booster inlet liquid separation tank, a hot low-pressure separation tank, a vacuum flash tank, a vacuum evaporator, a low-gas cooler, a flash tank top condenser, an evaporator freezer, a C9 alcohol separation tower and a heavy oil stripping tower;

[0030] The catalyst feed pipeline, the C8 olefin feed pipeline and the synthesis gas feed pipeline are all connected to the raw material reactor, the raw material reactor is provided with a hydroformylation reaction product outlet pipeline, the hydroformylation reaction product outlet pipeline is connected to the hot high-pressure separation tank, the hot high-pressure separation tank is provided with a high-fraction gas discharge pipeline and a hot high-pressure separation tank bottom liquid discharge pipeline, the high-fraction gas discharge pipeline is connected to the circulating synthesis gas booster inlet liquid separator, the circulating synthesis gas booster inlet liquid separator is provided with a synthesis gas discharge pipeline and a circulating synthesis gas booster inlet liquid separator bottom liquid discharge pipeline;

[0031] The hot high-pressure separation tank bottom liquid discharge pipeline and the circulating synthesis gas booster inlet liquid separation tank bottom liquid discharge pipeline are both connected to the hot low-pressure separation tank, the low-pressure separation tank is provided with a hot low-pressure separation tank bottom liquid discharge pipeline and a low-pressure separation tank top gas discharge pipeline, the low-pressure separation tank top gas discharge pipeline is connected to a low-pressure gas cooler, the low-pressure gas cooler is provided with a fuel gas discharge pipeline, the hot low-pressure separation tank bottom liquid discharge pipeline is connected to a vacuum flash tank, the vacuum flash tank is provided with a vacuum flash tank bottom liquid discharge pipeline and a vacuum flash tank top gas discharge pipeline, the top of the vacuum flash tank top gas discharge pipeline is connected to the flash tank top condenser, the flash tank top condenser is provided with a light component to torch C9 alcohol separation tower bottom liquid discharge pipeline, the vacuum flash tank bottom liquid discharge pipeline is connected to a vacuum evaporator, the vacuum evaporator is provided with a catalyst-containing C9 alcohol discharge pipeline and a vacuum evaporator top gas discharge pipeline;

[0032] The catalyst-containing C9 alcohol discharge pipeline is divided into two branches, one of which is connected to a heavy oil stripping tower, the heavy oil stripping tower is provided with a heavy oil discharge pipeline and a heavy oil stripping tower top gas discharge pipeline, the vacuum evaporator top gas discharge pipeline is connected to an evaporator freezer, and the evaporator freezer is provided with an evaporator top liquid discharge pipeline;

[0033] After the liquid discharge line at the top of the evaporator is merged with the gas discharge line at the top of the heavy oil stripping tower, it is connected to the C9 alcohol separation tower. The C9 alcohol separation tower is provided with a C8 gasoline discharge line and a liquid discharge line at the bottom of the C9 alcohol separation tower. The liquid discharge line at the bottom of the C9 alcohol separation tower is connected to the aldehyde hydrogenation unit.

[0034] In the present invention, the vacuum flash tank and the vacuum evaporator form a two-stage process of low vacuum flash evaporation-high vacuum evaporation. Flash evaporation under low vacuum removes most of the non-condensable gas, light components and water, reducing the load of the high vacuum system.

[0035] According to the present invention, preferably, the production unit also includes: a C8 olefin feed buffer tank, a catalyst preparation tank, a feedstock heater, a circulating C9 alcohol buffer tank, a product / circulating C9 alcohol heat exchanger, a catalyst activation reactor and a supplementary synthesis gas booster inlet separator tank.

[0036] Preferably, the C8 olefin feed pipeline is connected to a raw material heater, and the raw material heater is provided with a raw material heater discharge pipeline.

[0037] Preferably, after the catalyst feed pipeline is connected to the catalyst preparation tank, it merges with another catalyst-containing C9 alcohol discharge pipeline, and then connected to a circulating C9 alcohol buffer tank, and the circulating C9 alcohol buffer tank is provided with a circulating C9 alcohol buffer tank discharge pipeline.

[0038] Preferably, after the synthesis gas feed pipeline is connected to the inlet separator tank of the supplementary synthesis gas booster, it merges with the synthesis gas discharge pipeline of the inlet separator tank of the circulating synthesis gas booster and the discharge pipeline of the circulating C9 alcohol buffer tank, and then is sequentially connected to the product / circulating C9 alcohol heat exchanger and the catalyst activation reactor, and finally merges with the discharge pipeline of the raw material heater and is connected to the raw material reactor, and the liquid discharge pipeline at the bottom of the hot high-pressure separation tank is sequentially connected to the product / circulating C9 alcohol heat exchanger and the hot low-pressure separation tank.

[0039] According to the present invention, preferably, the feedstock reactor comprises 3 to 8 hydroformylation reactors;

[0040] Wherein, the hydroformylation reactor comprises:

[0041] A shell, wherein a reactant inlet is disposed at the lower portion of the shell, and a reactant outlet is disposed on the upper side wall of the shell;

[0042] a diffusion device, disposed inside the shell and above the reactant inlet, for dispersing the gaseous and liquid reaction medium entering the shell through the reactant inlet;

[0043] A distribution device, arranged inside the shell and above the diffusion device, and spaced apart from the diffusion device, for uniformly distributing the gas-liquid reaction medium;

[0044] A heat exchange distribution structure is arranged inside the shell and above the distribution device, and is spaced apart from the distribution device. The heat exchange distribution structure includes a plurality of heat exchange tubes and at least one distribution plate. The axes of the plurality of heat exchange tubes are parallel to each other. The plurality of heat exchange tubes are distributed in a ring shape along a plurality of concentric virtual circles. The distribution plate is provided with a plurality of positioning through holes and a distribution structure. The plurality of heat exchange tubes are respectively passed through the plurality of positioning through holes.

[0045] Optionally, the diffusion device includes a baffle and a plurality of connecting parts, two ends of the plurality of connecting parts are respectively connected to the reactant inlet and the baffle, and the baffle is in the shape of an inverted umbrella.

[0046] Optionally, a bubble generating device is further included, which is arranged outside the shell and connected to the reactant inlet, and is used to connect the gaseous reaction medium pipeline and the liquid reaction medium pipeline. A porous medium is arranged in the bubble generating device, and the gaseous reaction medium can enter the liquid reaction medium through the porous medium.

[0047] Optionally, a defoaming screen is further included, wherein the defoaming screen is arranged inside the shell and above the heat exchange distribution structure.

[0048] Optionally, the heat exchange tube includes an inner tube and an outer tube, and the two ends of the outer tube are respectively provided with a first sealing plate and a second sealing plate, one end of the inner tube is inserted into the outer tube and forms a first gap with the first sealing plate, and the other end of the inner tube passes through the second sealing plate and extends outward to form an extension portion, the outer end of the extension portion forms a heat exchange medium inlet, and a heat exchange medium outlet is opened on the outer wall of the outer tube.

[0049] Optionally, the heat exchange distribution structure also includes a first fixed baffle and a second fixed baffle connected to the inner wall of the shell at the outer periphery, the first fixed baffle is connected to the extension portion, the second fixed baffle is connected to the outer tube, a heat exchange medium inlet space is formed on the side of the first fixed baffle away from the second fixed baffle, a heat exchange medium outflow space is formed between the first fixed baffle and the second fixed baffle, the heat exchange medium inlet and the heat exchange medium outlet are respectively located in the heat exchange medium inlet space and the heat exchange medium outflow space, a cover plate is provided on the top of the heat exchange medium inlet space, a heat exchange medium pipeline is connected to the cover plate, a heat exchange medium total inlet connected to the heat exchange medium pipeline is provided on the top of the shell, and a heat exchange medium total outlet connected to the heat exchange medium outflow space is provided on the upper side wall of the shell.

[0050] Optionally, the distribution structure includes a plurality of distribution through holes, and the plurality of distribution through holes are opened on the distribution plate.

[0051] Optionally, the distribution plate is a slit mesh plate, and the slits and / or mesh holes of the slit mesh plate form the distribution structure.

[0052] Optionally, the distribution structure includes a plurality of tubular distributors, a plurality of mounting holes are provided on the distribution plate, and the plurality of tubular distributors are respectively installed on the reaction medium flow side of the distribution plate through the plurality of mounting holes. The tubular distributor includes a tube body and a buffer plate, one end of the tube body is connected to the mounting hole, a plurality of flow holes are provided on the outer wall of the tube body, a plurality of connecting pins are arranged at intervals on the outer periphery of the buffer plate, and the buffer plate is connected to the tube body through the connecting pins.

[0053] Optionally, the distribution device comprises a distribution plate, on which a distribution structure is arranged, the distribution structure is the same as the distribution structure, and the distribution structure and the distribution structure are arranged in a staggered manner.

[0054] The invention provides an isononanol hydroformylation reactor, which has the beneficial effects that: a diffusion device, a distribution device and a heat exchange distribution structure are sequentially arranged in a shell from bottom to top in the isononanol hydroformylation reactor; the diffusion device is arranged to buffer and disperse the gas-liquid reaction medium entering the shell through the reactant inlet, thereby preventing the gas-liquid reaction medium from being strongly mixed and impacted at the reactant inlet; the distribution device is arranged to evenly distribute the gas-liquid reaction medium, thereby improving the uniformity of the distribution of the gas-liquid reaction medium in the shell; the heat exchange distribution structure comprises a plurality of heat exchange tubes and at least one distribution plate; the plurality of heat exchange tubes are arranged in an annular shape along a plurality of concentric virtual circles. The distribution enables the gas-liquid reaction medium to flow in the axial direction of the heat exchange tube, i.e., the axial direction of the reactor, in a stable and flat push form, which is beneficial to the stability of the reaction mass transfer. A plurality of positioning through holes and a distribution structure are arranged on the distribution plate. The positioning through holes can position the heat exchange tube to form a support for the heat exchange tube, thereby ensuring the support strength of the heat exchange tube. The distribution structure can redistribute the gas-liquid reaction medium, and the downstream of the redistribution device can further improve the uniform distribution of the gas-liquid reaction medium, thereby achieving a stable and uniform distribution of gas and liquid in the reactor and improving the reaction conversion rate. The distribution form of the heat exchange tube and the coordination of the distribution plate can avoid the reverse mixing phenomenon while meeting the heat extraction conditions of the isononanol hydroformylation reaction.

[0055] The present invention has the following beneficial effects:

[0056] (1) The product separation unit removes most of the non-condensable steam, light components and water through a two-stage process of low vacuum flash evaporation and high vacuum evaporation, thereby reducing the load of the high vacuum system and saving energy consumption.

[0057] (2) The efficient and rapid catalyst separation process shortens the catalyst circulation path, which helps reduce catalyst decomposition.

[0058] (3) By using a vacuum evaporator, the material can be quickly separated at low pressure and low temperature, the catalyst circulation process is short, the separation temperature is low, and energy consumption is saved.

[0059] (4) Compared with the gradual vaporization sequential separation process, the production method of the present invention has a short catalyst cycle, less catalyst decomposition due to heat, and better economy.

[0060] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0061] The above and other objects, features and advantages of the present invention will become more apparent through a more detailed description of exemplary embodiments of the present invention in conjunction with the accompanying drawings, wherein like reference numerals generally represent like components throughout the exemplary embodiments of the present invention.

[0062] Figure 1A schematic diagram showing the production method of isononanol of the present invention.

[0063] Figure 2 A schematic diagram of a process flow diagram of a specific embodiment of the present invention is shown.

[0064] Figure 3 A schematic structural diagram of an isononanol hydroformylation reactor according to the present invention is shown.

[0065] Description of Reference Numerals

[0066] 1. C8 olefin feed buffer tank; 2. Catalyst preparation tank; 3. Raw material heater; 4. Raw material reactor; 5. Hot high-pressure separation tank; 6. Circulating C9 alcohol buffer tank; 7. Product / circulating C9 alcohol heat exchanger; 8. Catalyst activation reactor; 9. Supplementary synthesis gas booster inlet separator tank; 10. Circulating synthesis gas booster inlet separator tank; 11. Hot low-pressure separation tank; 12. Vacuum flash tank; 13. Vacuum evaporator; 14. Low-fraction gas cooler; 15. Flash tank top condenser; 16. Evaporator freezer; 17. Catalyst; 18. C9 alcohol separation tower bottom liquid; 19. C9 alcohol separation tower; 20. Aldehyde hydrogenation unit; 21. Heavy oil stripping tower; 22. C8 olefin; 23. Hydroformylation reaction product; 24. High-fraction gas; 25. C9 alcohol containing catalyst; 26. Synthesis gas; 27 , hot high-pressure separation tank bottom liquid; 28, circulating synthesis gas booster inlet separator tank bottom liquid; 29, C8 gasoline; 30, heavy oil; 31, hot low-pressure separation tank bottom liquid; 32, vacuum flash tank bottom liquid; 33, heavy oil stripping tower top gas; 34, vacuum evaporator top gas; 35, evaporator top liquid; 36, light component to flare C9 alcohol separation tower bottom liquid; 37, fuel gas; 38, isononanol product; 39, shell; 40, reactant inlet; 41, reactant outlet; 42, diffusion device; 43, distribution device; 44, heat exchange distribution structure; 45, bubble generating device; 46, defoaming wire mesh; 401, baffle; 402, connecting part; 601, heat exchange tube; 602, distribution plate; 614, total heat exchange medium inlet; 615, total heat exchange medium outlet. DETAILED DESCRIPTION

[0067] The preferred embodiments of the present invention will be described in more detail below. Although the preferred embodiments of the present invention are described below, it should be understood that the present invention can be implemented in various forms and should not be limited to the embodiments set forth herein.

[0068] Example 1

[0069] This embodiment adopts Figure 2According to the process flow shown in the figure, the C8 olefin 22 enters the C8 olefin feed buffer tank 1 for buffering, and then enters the raw material heater 3 for heating; the catalyst 17 enters the catalyst preparation tank 2 for preparation, and then is mixed with another part of the C9 alcohol 25 containing the catalyst, and then enters the circulating C9 alcohol buffer tank 6; the synthesis gas 26 enters the supplementary synthesis gas booster inlet separator tank 9 for pressurization, and then is mixed with the synthesis gas at the top of the circulating synthesis gas booster inlet separator tank 10 and the C9 alcohol 25 containing the catalyst at the outlet of the circulating C9 alcohol buffer tank 6, and then passes through the product / circulating C9 alcohol heat exchanger 7 to exchange heat with the liquid 27 at the bottom of the hot high-pressure separation tank. , enters the catalyst activation reactor 8 for activation, and finally is mixed with the C8 olefin 22 heated by the feed heater 3 and enters the feed reactor 4 for reaction to obtain a hydroformylation reaction product 23; the hydroformylation reaction product 23 enters the hot high-pressure separation tank 5 for gas-liquid separation to obtain a high-fraction gas 24 and a hot high-pressure separation tank bottom liquid 27, the high-fraction gas 24 enters the circulating synthesis gas booster inlet separator 10 for gas-liquid separation to obtain a synthesis gas 26 and a circulating synthesis gas booster inlet separator tank bottom liquid 28; the hot high-pressure separation tank bottom liquid 27 and the circulating synthesis gas booster inlet separator tank bottom liquid 28 both enter the hot The low-pressure separation tank 11 performs gas-liquid separation to obtain hot low-pressure separation tank bottom liquid 31 and hot low-pressure separation tank top gas, the hot low-pressure separation tank top gas enters the low-pressure gas cooler 14 for cooling to obtain fuel gas 37, the hot low-pressure separation tank bottom liquid 31 enters the vacuum flash tank 12 for gas-liquid separation to obtain vacuum flash tank bottom liquid 32 and vacuum flash tank top gas, the vacuum flash tank top gas enters the flash tank top condenser 15 for condensation to obtain light components to the torch C9 alcohol separation tower bottom liquid 36, the vacuum flash tank bottom liquid 32 is sent to the vacuum evaporator 13 for gas-liquid separation to obtain catalyst-containing C9 alcohol 2 5 and the top gas 34 of the vacuum evaporator; the C9 alcohol 25 containing the catalyst is divided into two parts, one part of which enters the heavy oil stripping tower 21 for gas-liquid separation to obtain heavy oil 30 and the top gas 33 of the heavy oil stripping tower, and the top gas 34 of the vacuum evaporator enters the evaporator freezer 16 for condensation to obtain the top liquid 35 of the evaporator; the top gas 33 of the heavy oil stripping tower and the top liquid 35 of the evaporator are mixed and then enter the C9 alcohol separation tower 19 for separation to obtain C8 gasoline 29 and the bottom liquid 18 of the C9 alcohol separation tower, and the bottom liquid 18 of the C9 alcohol separation tower is sent to the aldehyde hydrogenation unit 20 for reaction to obtain the isononanol product.

[0070] Among them, the operating conditions of the raw material reactor are: the reaction temperature is 180℃; the reaction pressure is 8.0MPag(g). The operating conditions of the product separation unit are: the operating temperature of the hot high-pressure separation tank is 180℃, and the operating pressure is 8MPag(g); the operating temperature of the hot low-pressure separation tank top is 50℃, the operating temperature of the tank bottom is 120℃, and the operating pressure is 0.5MPag(g); the operating temperature of the vacuum flash tank top is 10℃, the operating temperature of the tank bottom is 100℃, and the operating pressure is -0.1MPag(g); the operating temperature of the vacuum evaporator is 100℃, and the operating pressure is -0.1MPag(g); the operating temperature of the C9 alcohol separation tower top is 110℃, the operating temperature of the tower bottom is 210℃, and the operating pressure is 0.02MPag(g); the operating temperature of the heavy oil stripping tower top is 200℃, the operating temperature of the tower bottom is 230℃, and the operating pressure is 0.02MPag(g).

[0071] The material balance of Example 1 is shown in Table 1.

[0072] Table 1 Material balance

[0073]

[0074] As can be seen from Table 1, the two-stage process of low vacuum flash evaporation-high vacuum evaporation can effectively remove most of the non-condensable steam, light components and water.

[0075] Compared with the process without two-stage separation, the low vacuum flash-high vacuum evaporation two-stage process can reduce the high vacuum system load by more than 50%, and the vacuum system investment and energy consumption are reduced accordingly; compared with the traditional process, the energy consumption is reduced by more than 15% under the same vacuum degree. Compared with the traditional process, the rapid separation process shortens the catalyst circulation path and reduces the catalyst loss by more than 40%.

[0076] The embodiments of the present invention have been described above, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and changes will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. A method for producing isononyl alcohol, characterized in that: The steps include: C8 olefin (22), synthesis gas (26) and catalyst (17) enter into a raw material reactor (4) for reaction to obtain a hydroformylation reaction product (23); the hydroformylation reaction product (23) enters into a product separation unit for separation and removal of by-products, and then enters into an aldehyde hydrogenation unit (20) for reaction to obtain isononanol (38); The step of the hydroformylation reaction product (23) entering a product separation unit to separate and remove by-products comprises: The hydroformylation reaction product (23) enters the hot high-pressure separation tank (5) for gas-liquid separation to obtain high-fraction gas (24) and hot high-pressure separation tank bottom liquid (27); the high-fraction gas (24) enters the circulating synthesis gas booster inlet separation tank (10) for gas-liquid separation to obtain synthesis gas (26) and circulating synthesis gas booster inlet separation tank bottom liquid (28); the hot high-pressure separation tank bottom liquid (27) and the circulating synthesis gas booster inlet separation tank bottom liquid (28) both enter the hot low-pressure separation tank (11) for gas-liquid separation to obtain hot low-pressure separation tank bottom liquid (31) and hot low-pressure separation tank top gas. The hot low-pressure separation tank top gas enters the low-pressure gas cooler (14) for cooling to obtain fuel gas (37), the hot low-pressure separation tank bottom liquid (31) enters the vacuum flash tank (12) for gas-liquid separation to obtain vacuum flash tank bottom liquid (32) and vacuum flash tank top gas, the vacuum flash tank top gas enters the flash tank top condenser (15) for condensation to obtain light components to the flare C9 alcohol separation tower bottom liquid (36), the vacuum flash tank bottom liquid (32) is sent to the vacuum evaporator (13) for gas-liquid separation to obtain catalyst-containing C9 alcohol (25) and vacuum evaporator top gas (34); The catalyst-containing C9 alcohol (25) is divided into two parts, one part of which enters a heavy oil stripping tower (21) for gas-liquid separation to obtain heavy oil (30) and heavy oil stripping tower top gas (33), and the vacuum evaporator top gas (34) enters an evaporator freezer (16) for condensation to obtain evaporator top liquid (35); The heavy oil stripping tower top gas (33) and the evaporator top liquid (35) are mixed and then enter the C9 alcohol separation tower (19) for separation to obtain C8 gasoline (29) and C9 alcohol separation tower bottom liquid (18). The C9 alcohol separation tower bottom liquid (18) is sent to the aldehyde hydrogenation unit (20).

2. The method for producing isononyl alcohol according to claim 1, wherein The C8 olefin (22) enters the C8 olefin feed buffer tank (1) for buffering, then enters the feed heater (3) for heating, and then enters the feed reactor (4); The catalyst (17) enters the catalyst preparation tank (2) for preparation, is mixed with another portion of the catalyst-containing C9 alcohol (25), enters the circulating C9 alcohol buffer tank (6), and then enters the raw material reactor (4); After the synthesis gas (26) enters the inlet separator (9) of the supplementary synthesis gas compressor for pressurization, it is mixed with the synthesis gas at the top of the inlet separator (10) of the circulating synthesis gas compressor and the C9 alcohol (25) containing the catalyst at the outlet of the circulating C9 alcohol buffer tank (6), and then passes through the product / circulating C9 alcohol heat exchanger (7) to exchange heat with the liquid (27) at the bottom of the hot high-pressure separation tank, enters the catalyst activation reactor (8) for activation, and finally is mixed with the C8 olefin (22) heated by the feed heater (3) and enters the feed reactor (4).

3. The method for producing isononyl alcohol according to claim 1, wherein: The operating temperature of the hot high-pressure separation tank is 160-200°C and the operating pressure is 7-10MPag(g); The operating temperature of the top of the hot low-pressure separation tank is 30-60°C, the operating temperature of the bottom of the tank is 110-130°C, and the operating pressure is 0.2-1.5MPag(g).

4. The method for producing isononyl alcohol according to claim 1, wherein: The operating temperature of the vacuum flash tank top is 0-20°C, the operating temperature of the tank bottom is 80-120°C, and the operating pressure is -0.1-0.1MPag(g); The operating temperature of the vacuum evaporator is 800~120℃, and the operating pressure is -0.2~0.1MPag(g).

5. The method for producing isononyl alcohol according to claim 1, wherein: The operating temperature of the top of the heavy oil stripping tower is 180-210°C, the operating temperature of the bottom of the tower is 220-240°C, and the operating pressure is 0-0.2MPag(g); The operating temperature of the top of the C9 alcohol separation tower is 80-120°C, the operating temperature of the bottom of the tower is 190-220°C, and the operating pressure is 0-0.1MPag(g).

6. The method for producing isononyl alcohol according to claim 1, wherein: The C8 olefin (22), synthesis gas (26) and catalyst (17) enter 3 to 8 hydroformylation reactors for reaction.

7. The method for producing isononyl alcohol according to claim 6, wherein: The reaction temperature of each hydroformylation reactor is 160-200° C.; the reaction pressure is 7-10 MPag(g).

8. A production device for isononyl alcohol, characterized in that: The production device comprises: a catalyst feed pipeline, a C8 olefin feed pipeline, a synthesis gas feed pipeline, a raw material reactor (4), a product separation unit and an aldehyde hydrogenation unit (20); The product separation unit comprises: a hot high-pressure separation tank (5), a circulating synthesis gas booster inlet liquid separation tank (10), a hot low-pressure separation tank (11), a vacuum flash tank (12), a vacuum evaporator (13), a low-pressure gas cooler (14), a flash tank top condenser (15), an evaporator freezer (16), a C9 alcohol separation tower (19) and a heavy oil stripping tower (21); The catalyst feed pipeline, the C8 olefin feed pipeline and the synthesis gas feed pipeline are all connected to the raw material reactor (4), the raw material reactor (4) is provided with a hydroformylation reaction product outlet pipeline, the hydroformylation reaction product outlet pipeline is connected to the hot high-pressure separation tank (5), the hot high-pressure separation tank (5) is provided with a high-gas discharge pipeline and a hot high-pressure separation tank bottom liquid discharge pipeline, the high-gas discharge pipeline is connected to the circulating synthesis gas booster inlet liquid separator (10), the circulating synthesis gas booster inlet liquid separator (10) is provided with a synthesis gas discharge pipeline and a circulating synthesis gas booster inlet liquid separator bottom liquid discharge pipeline; The hot high-pressure separation tank bottom liquid discharge pipeline and the circulating synthesis gas booster inlet liquid separation tank bottom liquid discharge pipeline are both connected to the hot low-pressure separation tank (11), the low-pressure separation tank (11) is provided with a hot low-pressure separation tank bottom liquid discharge pipeline and a low-pressure separation tank top gas discharge pipeline, the low-pressure separation tank top gas discharge pipeline is connected to a low-pressure gas cooler (14), the low-pressure gas cooler (14) is provided with a fuel gas discharge pipeline, the hot low-pressure separation tank bottom liquid discharge pipeline is connected to a vacuum flash tank (12), The vacuum flash tank (12) is provided with a vacuum flash tank bottom liquid discharge pipeline and a vacuum flash tank top gas discharge pipeline, the top of the vacuum flash tank top gas discharge pipeline is connected to the flash tank top condenser (15), the flash tank top condenser (15) is provided with a light component to the flare C9 alcohol separation tower bottom liquid discharge pipeline, the vacuum flash tank bottom liquid discharge pipeline is connected to the vacuum evaporator (13), the vacuum evaporator (13) is provided with a catalyst-containing C9 alcohol discharge pipeline and a vacuum evaporator top gas discharge pipeline; The catalyst-containing C9 alcohol discharge pipeline is divided into two branches, one of which is connected to a heavy oil stripping tower (21), the heavy oil stripping tower (21) is provided with a heavy oil discharge pipeline and a heavy oil stripping tower top gas discharge pipeline, the vacuum evaporator top gas discharge pipeline is connected to an evaporator freezer (16), and the evaporator freezer (16) is provided with an evaporator top liquid discharge pipeline; After the liquid discharge pipeline at the top of the evaporator is merged with the gas discharge pipeline at the top of the heavy oil stripping tower, it is connected to the C9 alcohol separation tower (19). The C9 alcohol separation tower (19) is provided with a C8 gasoline discharge pipeline and a liquid discharge pipeline at the bottom of the C9 alcohol separation tower. The liquid discharge pipeline at the bottom of the C9 alcohol separation tower is connected to the aldehyde hydrogenation unit (20).

9. The production device of isononyl alcohol according to claim 8, wherein: The production device also includes: a C8 olefin feed buffer tank (1), a catalyst preparation tank (2), a feed heater (3), a circulating C9 alcohol buffer tank (6), a product / circulating C9 alcohol heat exchanger (7), a catalyst activation reactor (8) and a supplementary synthesis gas booster inlet separator tank (9); The C8 olefin feed pipeline is connected to a raw material heater (3), and the raw material heater (3) is provided with a raw material heater discharge pipeline; After the catalyst feed pipeline is connected to the catalyst preparation tank (2), it merges with another catalyst-containing C9 alcohol discharge pipeline, and then connected to the circulating C9 alcohol buffer tank (6), and the circulating C9 alcohol buffer tank (6) is provided with a circulating C9 alcohol buffer tank discharge pipeline; After the synthesis gas feed pipeline is connected to the supplementary synthesis gas booster inlet separator (9), it merges with the synthesis gas discharge pipeline of the circulating synthesis gas booster inlet separator (10) and the discharge pipeline of the circulating C9 alcohol buffer tank, and then sequentially connected to the product / circulating C9 alcohol heat exchanger (7) and the catalyst activation reactor (8), and finally merges with the discharge pipeline of the raw material heater and is connected to the raw material reactor (4). The hot high-pressure separation tank bottom liquid discharge pipeline is sequentially connected to the product / circulating C9 alcohol heat exchanger (7) and the hot low-pressure separation tank (11).

10. The production device of isononyl alcohol according to claim 8, wherein: The raw material reactor (4) includes 3 to 8 hydroformylation reactors; Wherein, the hydroformylation reactor comprises: A shell (39), wherein a reactant inlet (40) is disposed at a lower portion of the shell, and a reactant outlet (41) is disposed on an upper side wall of the shell; a diffusion device (42), arranged inside the shell and above the reactant inlet, for dispersing the gaseous and liquid reaction medium entering the shell through the reactant inlet; A distribution device (43) is arranged inside the shell and above the diffusion device, and is spaced apart from the diffusion device, and is used to evenly distribute the gas-liquid reaction medium; A heat exchange distribution structure (44) is arranged inside the shell and above the distribution device, and is spaced apart from the distribution device. The heat exchange distribution structure includes a plurality of heat exchange tubes (601) and at least one distribution plate (602). The axes of the plurality of heat exchange tubes are parallel to each other. The plurality of heat exchange tubes (601) are distributed in a ring shape along a plurality of concentric virtual circles. The distribution plate is provided with a plurality of positioning through holes and a distribution structure. The plurality of heat exchange tubes are respectively inserted into the plurality of positioning through holes.

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