WO2022148162A1 - 一种反应装置及羰基合成醋酸的系统和方法 - Google Patents

一种反应装置及羰基合成醋酸的系统和方法 Download PDF

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WO2022148162A1
WO2022148162A1 PCT/CN2021/132466 CN2021132466W WO2022148162A1 WO 2022148162 A1 WO2022148162 A1 WO 2022148162A1 CN 2021132466 W CN2021132466 W CN 2021132466W WO 2022148162 A1 WO2022148162 A1 WO 2022148162A1
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circulating fluid
gas distribution
stirring
gas
reaction
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PCT/CN2021/132466
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English (en)
French (fr)
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陈大胜
顾明兰
刘文艳
吴良泉
孟庆军
顾卫忠
钱永明
金庸
凌国珍
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上海华谊能源化工有限公司
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/06—Flash distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/085—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/10—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide
    • C07C51/12—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide on an oxygen-containing group in organic compounds, e.g. alcohols
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Definitions

  • the invention belongs to the field of chemical industry, and relates to a reaction device and a system and method for synthesizing acetic acid by carbonyl.
  • Acetic acid is an important chemical intermediate and solvent for chemical reactions.
  • the most commonly used one is the methanol low-pressure oxo synthesis process, which was pioneered by the American Monsanto Company in the 1970s.
  • Traditional gas-liquid stirring and mixing mostly adopts conventional mechanical stirring mode.
  • the reaction equipment using mechanical stirring can effectively carry out liquid-liquid and gas-liquid mixing.
  • the shaft seals and bearings required for mechanical transmission are easily damaged in long-term operation. It is difficult to achieve continuous, stable and safe operation due to shutdown maintenance.
  • the use of hydraulic agitation has become an important direction for the technical improvement of methanol oxo-acetic acid plants.
  • the use of hydraulic agitation technology mainly has the following problems: the single-layer annular distributor has uneven gas distribution, which causes catalyst precipitation; liquid Uneven distribution leads to uneven reaction and uneven temperature field distribution; production capacity decreases, etc.
  • the object of the present invention is to provide a reaction device and a system and method for oxo acetic acid, adopt the reaction device of the present invention to carry out oxo acetic acid production, avoid shaft sealing and bottom fixing in mechanical stirring
  • the bearing is easily damaged during operation.
  • at least one gas distribution stirring unit distributed in multiple layers and connected in sequence makes the reaction kettle more efficient than the existing single-layer distributor.
  • the gas distribution inside is more uniform, the mixing effect of gas-liquid two-phase is improved, the reaction rate is increased, and the internal reaction state of the system is optimized.
  • a first aspect of the present invention provides a reaction device, comprising a reaction kettle, a circulating fluid stirring part and a raw material gas distribution stirring part;
  • the reaction kettle includes a raw material gas feeding pipe, and the reaction kettle is provided with a raw material gas inlet and a circulating fluid outlet , at least one circulating fluid inlet;
  • the circulating fluid stirring part comprises at least one circulating fluid feeding pipe;
  • the gas distribution stirring part is arranged in the reaction kettle, and the gas distribution stirring part comprises at least one gas distribution stirring unit;
  • the circulating fluid feed pipe penetrates the circulating fluid inlet and communicates with the circulating fluid outlet;
  • the raw gas feeding pipe penetrates the raw gas inlet and communicates with the gas distribution and stirring part.
  • the vertical distance between the circulating fluid feed pipe and the central axis of the reactor is 0-3*D/8, and D is the diameter of the reactor;
  • the included angle of the vertical projection of the central axis of the adjacent circulating fluid feed pipes on the radial plane of the reactor is 60° to 150°, such as 60° to 120° or 120°. ° ⁇ 150°.
  • the gas distribution stirring unit includes at least one of the following technical features:
  • the gas distribution stirring unit is annular, and is arranged symmetrically along the central axis of the reaction kettle;
  • two or more gas distribution stirring units are distributed and communicated in multiple layers along the central axis of the reactor, from the bottom gas distribution stirring unit near the inlet end of the raw material gas to the farthest raw material gas
  • the diameters of the gas distribution stirring units of each layer increase in turn;
  • D is the diameter of the reaction kettle
  • Dni is the outer diameter of the n i layer gas distribution stirring unit
  • n i 1
  • the gas distribution stirring unit is the closest to the inlet end of the raw material gas
  • the gas distribution stirring unit at the inlet end of the raw material gas starts to count the number of layers
  • n is the total number of layers of the gas distribution stirring parts.
  • the gas distribution and stirring units of each layer are connected in sequence.
  • the gas distribution stirring unit is provided with uniformly symmetrical or staggered distribution pores
  • reaction kettle is also provided with a reaction solution outlet for outputting the reaction solution;
  • the raw material gas inlet is located at the bottom of the reactor;
  • the circulating fluid inlet is located at the top of the reactor;
  • the circulating fluid stirring component further includes a circulating fluid pump and/or a circulating fluid heat exchanger, and the circulating fluid outlet is connected to the circulating fluid through the circulating fluid pump and/or the circulating fluid heat exchanger through at least one passage, respectively. the at least one circulating fluid feed pipe is connected;
  • the diameter of the air hole is 2mm ⁇ 10mm, such as 2mm ⁇ 6mm, 6mm ⁇ 7mm or 7mm ⁇ 10mm;
  • the air hole spacing is 20mm to 60mm;
  • the nozzle is located in the middle of the reactor;
  • the nozzle is a diameter-reducing structure
  • the nozzle is located 1/6H ⁇ 1/2H below the liquid level of the reaction device, such as 1/6H ⁇ 2/6H, 2/6H ⁇ 2/5H, 2/5H ⁇ 1/2H, wherein , H is the length of the straight side of the barrel of the reactor;
  • the circulating fluid stirring component includes at least one circulating fluid pump and/or at least one circulating fluid heat exchanger, and the circulating fluid outlet is divided into at least one passageway and the at least one circulating fluid feeding pipe respectively. Connection, a circulating fluid pump and/or a circulating fluid heat exchanger are provided on a single passage.
  • a second aspect of the present invention provides a system for oxo-synthesizing acetic acid, comprising the above-mentioned reaction device, a flash separator and a refining unit connected in sequence.
  • the flash separator is provided with a gas phase outlet and a liquid phase outlet, the gas phase outlet communicates with the refining unit, and the liquid phase outlet communicates with the reaction device.
  • a third aspect of the present invention provides a method for oxo-synthesizing acetic acid, which adopts the above-mentioned reaction device, feeds reaction raw materials including methanol, CO and a catalyst into the reaction device, and adopts the circulating fluid stirring part and the gas distribution stirring part And the material is stirred to react under the action of a catalyst to generate acetic acid.
  • reaction solution is separated by flash evaporation to obtain gas-phase material and liquid-phase material respectively;
  • gas-phase material is purified to obtain an acetic acid product, and the liquid-phase material is returned to the reaction device;
  • the flow velocity at the outlet of the gas distribution stirring unit is 5m/s ⁇ 30m/s, such as 5m/s ⁇ 7m/s, 7m/s ⁇ 15m/s, 15m/s ⁇ 20m/s, 20m/s ⁇ 25m/s s or 25m/s ⁇ 30m/s;
  • the fluid flow rate sprayed by the nozzle of the circulating fluid feed pipe is 5m/s ⁇ 20m/s, such as 5m/s ⁇ 11m/s, 11m/s ⁇ 15m/s or 15m/s ⁇ 20m/s; circulating fluid
  • the nozzle at the end of the circulating fluid feed pipe is sprayed at a high speed, which drives the surrounding liquid to change the vector, and turns up from the bottom of the reactor, causing greater disturbance to the liquid in the reactor.
  • Multiple large circulating flow states are formed in the reactor to ensure that the liquid in the entire reactor is evenly mixed, so as to achieve uniform distribution of the concentration field and temperature field of the liquid in the reactor;
  • the total fluid flow per hour at the outlet of two or more circulating fluid feed pipes is 5 to 10 times the volume of the reaction liquid, such as 5 to 6.2 times, 6.2 to 7.5 times, or 7.5 to 10 times.
  • the reaction device of the invention comprises a circulating fluid stirring part and a raw gas distribution stirring part, and is used in the production of methanol low-pressure oxo-acetic acid.
  • There is no dynamic sealing point in the whole reaction device which eliminates the hidden danger of shutdown caused by mechanical agitation caused by the leakage of the mechanical seal and the internal pressure of the kettle.
  • the stirring parts need to be replaced due to corrosion, which ensures the safe and stable operation of the reaction system, and saves the expenditure of investment, operation and maintenance costs;
  • the three-dimensional multi-layer ring-shaped raw gas distribution stirring parts make the gas distribution in the reactor more uniform and improve the gas
  • the liquid two-phase mixing effect optimizes the internal reaction state of the system, reduces the temperature difference in the reactor, and reduces side reactions;
  • the configured fluid circulation stirring system makes the liquid distribution more uniform, the temperature field in the reactor is more uniform, and the production is more stable and the production capacity is obtained. promote.
  • Fig. 1 is the structural schematic diagram 1 of the reaction device of the present invention.
  • Fig. 2 is the second structural schematic diagram of the reaction device of the present invention.
  • FIG 3 is a schematic top view of the structure of two circulating fluid feed pipes in the circulating fluid stirring component of the present invention.
  • FIG. 4 is a schematic top view of the structure of the gas distribution stirring component of the present invention.
  • Figure 5 is a systematic diagram of the oxo synthesis of acetic acid.
  • Fig. 6 is a schematic side view of the structure of a single circulating fluid feed pipe in the circulating fluid stirring component of the present invention.
  • a reaction device as shown in Figures 1 and 2, includes a reaction kettle 11, a circulating fluid stirring part 12 and a raw material gas distribution stirring part 13;
  • the reaction kettle 11 includes a raw material gas feeding pipe 1111, and the reaction kettle 11 It is provided with a raw material gas inlet 1112, a circulating fluid outlet 1121, and at least one circulating fluid inlet 1122;
  • the circulating fluid stirring part 12 includes at least one circulating fluid feeding pipe 121;
  • the gas distribution stirring part 13 is provided in the reaction kettle 11 Inside, the gas distribution stirring part 13 includes at least one gas distribution stirring unit 131;
  • the circulating fluid feeding pipe 121 penetrates the circulating fluid inlet 1122 and communicates with the circulating fluid outlet 1121;
  • the raw gas feeding pipe 1111 penetrates through the raw material gas inlet 1112 and communicates with the gas distribution stirring member 13 .
  • the use of three-dimensional multi-layer gas distribution and stirring components facilitates the uniform distribution of CO gas on the cross-section of the reaction kettle 11.
  • the CO gas moves upward from the pores of different heights to reduce the phenomenon of CO bubble coalescence, so that the CO gas in the entire reaction kettle 11 is
  • the existence of smaller bubbles reduces the diffusion resistance of CO into the liquid, ensures that the gas distribution in the reactor 11 is relatively uniform, and improves the mixing effect of the gas-liquid two phases.
  • the vertical distance between the circulating fluid feed pipe 121 and the central axis of the reactor is 0 ⁇ 3*D/8, D is the diameter of the reactor.
  • the uniformity of the liquid in one circulating fluid feed pipe is good, so that the temperature field and the concentration field are more uniform, the side reactions are less, and the production capacity can be higher.
  • the included angle between the vertical projections of the central axes of adjacent circulating fluid feeding pipes 121 on the radial plane of the reactor is 60° ⁇ 150°, the included angle is ⁇ in Figure 3. This design ensures that the liquid in the reactor is more uniform, the reaction in the reactor is more uniform, the temperature difference is reduced, and the side reactions are reduced.
  • the gas distribution stirring unit 131 is annular, and is arranged symmetrically along the central axis of the reaction kettle.
  • the two or more gas distribution stirring units 131 are distributed and communicated in multiple layers along the central axis of the reactor. From the bottom layer gas distribution stirring unit at the raw material gas inlet end to the top layer gas distribution stirring unit at the far raw material gas inlet end, the diameters of the gas distribution stirring units 131 in each layer increase sequentially.
  • the calculation formula of the diameter of the gas distribution stirring unit 131 is as follows:
  • D is the diameter of the reaction kettle
  • Dni is the outer diameter of the n i layer gas distribution stirring unit
  • n i 1
  • the gas distribution stirring unit is the closest to the inlet end of the raw material gas
  • the gas distribution stirring unit at the inlet end of the raw material gas starts to count the number of layers
  • n is the total number of layers of the gas distribution stirring parts.
  • the gas distribution and stirring member 13 is a multi-layer annular pipe body interconnected structure.
  • the sum of the distances between adjacent gas distribution and stirring units + the distance between the bottom gas distribution and stirring units and the bottom of the reactor ⁇ the radius of the reactor.
  • the height between the bottom of the reaction kettle and the bottom layer gas distribution and stirring unit, namely the first layer ring is H1
  • the bottom gas distribution stirring unit is the height between the first layer ring and the second layer ring is H2
  • the second layer ring is H2.
  • the height between the ring and the third layer ring is H3
  • the height between the n-1th layer ring and the nth layer ring is Hn
  • H1+H2+H3+...Hn the radius of the reaction kettle.
  • the gas distribution and stirring units 131 of each layer are connected in sequence.
  • the gas distribution stirring unit 131 is provided with uniformly symmetrical or staggered air holes 1311 .
  • the diameter of the air hole is 2mm-10mm, such as 2mm-6mm, 6mm-7mm or 7mm-10mm.
  • the air hole spacing is 20mm ⁇ 60mm.
  • reaction kettle 11 is further provided with a reaction liquid outlet for outputting the reaction liquid.
  • a nozzle 1211 is provided at the end of the circulating fluid feed pipe 121 provided in the reactor 11.
  • the spray head 1211 is located in the middle of the reaction kettle 11 .
  • the nozzle 1211 is of a reduced diameter structure. This design can ensure that the liquid at the nozzle outlet spews out at a higher speed.
  • the spray head 1211 is located 1/6H ⁇ 1/2H below the liquid level of the reaction device, such as 1/6H ⁇ 2/6H, 2/6H ⁇ 2/5H, 2/5H ⁇ 1/2H , where H is the length of the straight side of the barrel of the reactor.
  • the raw material gas inlet 1112 is provided at the bottom of the reactor 11 .
  • the circulating fluid outlet 1121 is provided in the middle of the reactor 11 .
  • the circulating fluid inlet 1122 is provided at the top of the reactor 11 .
  • the circulating fluid stirring member 12 further includes a circulating fluid pump 122 and/or a circulating fluid heat exchanger 123, and the circulating fluid outlet 1121 passes through the circulating fluid pump 122 and/or the circulating fluid
  • the fluid heat exchangers 123 are respectively connected with the at least one circulating fluid feed pipe 121 in at least one passage.
  • the circulating fluid outlet is connected to a circulating fluid pump 122. After being cooled by a circulating fluid heat exchanger 123, it is divided into at least one stream and enters the reactor through at least one circulating fluid feeding pipe 121. The nozzle of the upper part is sprayed at a high speed to achieve uniform stirring and mixing of the liquid in the reaction kettle.
  • the circulating fluid stirring member 12 includes at least one circulating fluid pump 122 and/or at least one circulating fluid heat exchanger 123, and the circulating fluid outlet 1121 is divided into at least one passageway with the at least one circulating fluid outlet 1121 respectively.
  • the circulating fluid feed pipe 121 is connected, and a circulating fluid pump 122 and/or a circulating fluid heat exchanger 123 are arranged on a single passage.
  • the circulating fluid outlet is divided into two parts, which are respectively connected to a circulating fluid pump 122. After being cooled by the circulating fluid heat exchanger 123, respectively, they enter the reactor through two circulating fluid feeding pipes 121.
  • the circulating fluid outlet is one, connected to a circulating fluid pump 122. After being cooled by a circulating fluid heat exchanger 123, it enters the reactor through a circulating fluid feeding pipe 121. It is sprayed at a high speed to achieve uniform stirring and mixing of the liquid in the reactor.
  • the raw material gas distribution and stirring member 13 is provided at the bottom of the reaction kettle 11 .
  • a second aspect of the present invention provides a system for oxo-synthesizing acetic acid, as shown in FIG. 5 , comprising the above-mentioned reaction device 1 , a flash separator 2 and a refining unit 3 that are connected in sequence.
  • the flash separator 2 is provided with a gas phase outlet 21 and a liquid phase outlet 22 , the gas phase outlet 21 communicates with the refining unit 3 , and the liquid phase outlet 22 communicates with the reaction device 1 .
  • the following embodiments 1 to 3 adopt a preferred reaction device, as shown in Figure 1, Figure 3 and Figure 4, comprising a reaction kettle 11, a circulating fluid stirring part 12 and a raw gas distribution stirring part 13;
  • the reaction kettle 11 Including a raw material gas feeding pipe 1111, the reaction kettle 11 is provided with a raw material gas inlet 1112, a circulating fluid outlet 1121, and at least one circulating fluid inlet 1122;
  • the circulating fluid stirring part 12 includes at least one circulating fluid feeding pipe 121;
  • the gas distribution stirring part 13 is arranged in the reaction kettle 11, and the gas distribution stirring part 13 includes at least one gas distribution stirring unit 131;
  • the circulating fluid feeding pipe 121 penetrates the circulating fluid inlet 1122 and is connected with the The circulating fluid outlet 1121 is in communication;
  • the raw material gas feeding pipe 1111 penetrates the raw material gas inlet 1112 and communicates with the gas distribution stirring part 13 .
  • the gas distribution stirring units 131 are annular and arranged symmetrically along the central axis of the reactor; when there are more than two gas distribution stirring units 131, two or more gas distribution stirring units 131 are distributed in multiple layers along the central axis of the reactor And connected, from the bottom gas distribution stirring unit near the raw material gas inlet end to the top gas distribution stirring unit far from the raw material gas inlet end, the diameter of each layer of gas distribution stirring unit 131 increases in turn, and the gas distribution stirring unit 131
  • the calculation formula for the diameter of the unit is as follows :
  • D is the diameter of the reaction kettle
  • Dni is the outer diameter of the n i layer gas distribution stirring unit
  • n i 1
  • the gas distribution stirring unit is the closest to the inlet end of the raw material gas
  • the gas distribution stirring unit at the inlet end of the raw material gas starts to count the number of layers
  • n is the total number of layers of the gas distribution stirring parts. From the bottom layer gas distribution and stirring unit near the raw material gas inlet end to the top layer gas distribution and stirring unit far from the raw material gas inlet end, the gas distribution and stirring units 131 of each layer are connected in sequence.
  • the reaction kettle 11 is also provided with a reaction liquid outlet for outputting the reaction liquid.
  • a nozzle 1211 is provided at the end of the circulating fluid feed pipe 121 in the reaction kettle 11 .
  • the spray head 1211 is located in the middle of the reactor 11 .
  • the nozzle 1211 is of a reduced diameter structure.
  • the nozzle 1211 is located at 1/6H to 1/2H below the liquid level of the reaction device, wherein H is the length of the straight side of the cylinder of the reaction kettle.
  • the raw material gas inlet 1112 is located at the bottom of the reactor 11 .
  • the circulating fluid outlet 1121 is located in the middle of the reactor 11 .
  • the circulating fluid inlet 1122 is provided at the top of the reactor 11 .
  • the circulating fluid stirring part 12 further includes a circulating fluid pump 122 and a circulating fluid heat exchanger 123, and the circulating fluid outlet 1121 is respectively connected with the circulating fluid pump 122 and the circulating fluid heat exchanger 123 through at least one passageway.
  • the at least one circulating fluid feed pipe 121 is connected.
  • the raw material gas distribution and stirring member 13 is arranged at the bottom of the reaction kettle 11 .
  • the industrial plant for the synthesis of acetic acid at low pressure from methanol Before the transformation of the reactor, a mechanical stirring device was used. The height of the reactor barrel was 5m and the diameter was 3m. The diameter of the air hole is 15mm, the diameter of the outer circle is 1m, and the outlet of the circulating fluid feeding pipe (one) is located above the liquid level and has no diameter reduction.
  • methanol and CO undergo carbonylation reaction to generate acetic acid, and the temperature difference in the axial direction of the reactor is about 3 °C.
  • the methanol low-pressure synthesis acetic acid reaction device the height of the reactor barrel (that is, the length of the straight side of the barrel of the reactor) is 5m, and the diameter is 3m.
  • the circulating fluid shown in Figure 1, Figure 3 and Figure 4 is used to stir Parts and three-dimensional multi-ring raw material gas distribution and stirring parts, the included angle between the vertical projections of the central axes of the two circulating fluid feeds on the radial plane of the reactor is 150°, and the end nozzles of the two circulating fluid feeding pipes are located at At 5/6m below the liquid level (1/6 of the length of the straight side of the barrel of the reactor), the fluid flow rate from the nozzle of the circulating fluid feed pipe is 5m/s, and the total fluid flow at the outlet of the circulating fluid feed pipe is 200 m 3 /h, 5 times the volume of the reaction solution.
  • the raw gas distribution stirring component includes two gas distribution stirring units 131, namely two layers, with outer diameters of 1 m and 2 m respectively.
  • the gas distribution stirring unit is provided with uniform and symmetrical air holes, the diameter of the air holes is 6 mm, and the average gas velocity of the air outlet is 5m/s, the sum of the distances between adjacent gas distribution stirring units + the bottom layer gas distribution stirring unit, that is, the distance between the first layer gas distribution stirring unit and the bottom of the reaction kettle is 1.2m.
  • the axial temperature of the reactor is reduced by 2 °C relative to the comparative example, that is, the axial temperature difference of the reactor is about 1 °C.
  • the propionic acid content was reduced by 100 ppm.
  • the methanol low-pressure synthesis acetic acid reaction device the height of the reactor barrel is 5m, the diameter is 3m, after the reactor is transformed, the circulating fluid stirring part and the three-dimensional multi-ring raw material gas distribution stirring part shown in Figure 2, Figure 3 and Figure 4 are used.
  • the raw gas distribution and stirring component includes three gas distribution and stirring units 131, namely three layers, with outer diameters of 0.75m, 1.5m and 2.25m respectively.
  • the gas distribution and stirring units are provided with uniform and symmetrical air holes, the diameter of the air holes is 10mm, and the air outlet holes are 10mm in diameter.
  • the average gas velocity is 15m/s, and the total distance between adjacent gas distribution stirring units + the bottom gas distribution stirring unit, that is, the distance between the first layer gas distribution stirring unit and the bottom of the reactor is 1.0m.
  • the axial temperature of the reactor is reduced by 1°C relative to the comparative example, that is, the axial temperature difference of the reactor is about 2°C.
  • the propionic acid content was reduced by 70 ppm.
  • the methanol low-pressure synthesis acetic acid reaction device the height of the reactor barrel is 5m, the diameter is 3m, after the reactor is transformed, the circulating fluid stirring part and the three-dimensional multi-ring raw material gas distribution stirring part shown in Figure 2, Figure 3 and Figure 4 are used.
  • the raw gas distribution stirring component includes four gas distribution stirring units 131, namely four layers, with outer diameters of 0.6m, 1.2m, 1.8m, and 2.4m, respectively.
  • the gas distribution and stirring units are provided with There are uniform and symmetrical air holes, the diameter of the air holes is 2mm, the average gas velocity of the air holes is 20m/s, the sum of the distances between the adjacent gas distribution stirring units + the bottom gas distribution stirring unit, that is, the first layer gas distribution stirring unit and the bottom of the reactor.
  • the spacing is 1.2m.
  • methanol and CO undergo carbonylation reaction to generate acetic acid
  • the axial temperature of the reactor is reduced by 0.5 °C relative to the comparative example, that is, the axial temperature difference of the reactor is about 2.5 °C.
  • the propionic acid content was reduced by 80 ppm.
  • the methanol low-pressure synthesis acetic acid reaction device the height of the reactor barrel is 5m, the diameter is 3m, after the reactor is transformed, the circulating fluid stirring part and the three-dimensional multi-ring raw material gas distribution stirring part shown in Figure 2, Figure 3 and Figure 4 are used.
  • the included angle of the vertical projection of the central axis of the two circulating fluid feed pipes on the radial plane of the reactor is 120°
  • the end nozzles of the two circulating fluid feeding pipes are located at 12/6 below the liquid level (for the reaction 2/5 of the length of the straight side of the barrel of the kettle)
  • the fluid flow rate that the nozzle of the circulating fluid feed pipe spouts is 20m/s
  • the total flow of the outlet fluid of the circulating fluid feed pipe is 423m 3 /h, which is the 10 times
  • the raw gas distribution stirring part includes five gas distribution stirring units 131, namely five layers
  • the outer diameters are 0.5m, 1m, 1.5m, 2m, 2.5m respectively
  • the gas distribution and stirring units are provided with uniform and symmetrical air holes.
  • the diameter of the air hole is 7mm, the average gas velocity of the air outlet is 30m/s, the sum of the distance between adjacent gas distribution stirring units + the bottom gas distribution stirring unit, that is, the distance between the first layer gas distribution stirring unit and the bottom of the reactor is 1.4m.
  • the axial temperature of the reactor is reduced by 2.5 °C relative to the comparative example, that is, the axial temperature difference of the reactor is about 0.5 °C.
  • Propionic acid content decreased by 120ppm.

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Abstract

本发明提供一种反应装置，包括反应釜、循环流体搅拌部件和原料气体分布搅拌部件；气体分布搅拌部件包括至少一个气体分布搅拌单元；循环流体进料管贯穿循环流体进口并与循环流体出口连通；原料气体进料管贯穿原料气体进口并与气体分布搅拌部件连通。采用该反应装置进行羰基合成醋酸，避免机械搅拌中轴封及底部固定轴承在运行过程中易损坏，没有动密封点，保障反应系统安全稳定运行；适宜的内构件尺寸和工艺操作指标确保液体分布的均匀性，保证运行过程工况的稳定性；同时多层分布且依次连通的至少一个气体分布搅拌单元使反应釜内的气体分布更加均匀，改善气液两相混合效果，优化系统内部反应状态，反应釜内温差减小，副反应减少。

Description

一种反应装置及羰基合成醋酸的系统和方法 技术领域
本发明属于化工领域，涉及一种反应装置及羰基合成醋酸的系统和方法。
背景技术
醋酸是一种重要的化学中间体和化学反应用溶剂。在目前投用的醋酸合成的工艺中，最常用的一种是甲醇低压羰基合成工艺，该工艺由美国孟山都公司在70年代首创，经过几十年的革新发展，装置产能、产品质量、生产成本均取得了重大突破。传统气液搅拌混合多采用常规机械搅拌模式，采用机械搅拌的反应设备可以有效地进行液-液和气-液的混合，但是，机械传动所需的轴封和轴承在长期运行中极易损坏，造成停车维修，难以实现持续、稳定和安全地运行。近几年，使用液力搅拌成为甲醇羰基合成醋酸装置技术改进的一个重要方向，目前使用液力搅拌技术主要存在如下问题：单层环式分布器存在气体分布不均，从而引起催化剂沉淀；液体分布不均匀，导致反应不均匀，温度场分布不均；生产产能下降等。
发明内容
针对上述现有技术中存在的技术问题，本发明的目的是提供一种反应装置及羰基合成醋酸的系统和方法，采用本发明反应装置进行羰基合成醋酸生产，避免机械搅拌中轴封及底部固定轴承在运行过程中易损坏的现象，整个反应装置中没有动密封点，保障反应系统安全稳定运行；同时多层分布且依次连通的至少一个气体分布搅拌单元比现有单层分布器使反应釜内的气体分布更加均匀，改善气液两相混合效果，提升反应速率，优化系统内部反应状态。
本发明是通过以下技术方案实现的：
本发明第一方面提供一种反应装置，包括反应釜、循环流体搅拌部件和原料气体分布搅拌部件；所述反应釜包括原料气体进料管，所述反应釜设有原料气体进口、循环流体出口、至少一个循环流体进口；所述循环流体搅拌部件包括至少一个循环流体进料管；所述气体分布搅拌部件设于所述反应釜内，所述气体分布搅拌部件包括至少一个气体分布搅拌单元；所述循环流体进料管贯穿所述循环流体进口并与所述循环流体出口连通；所述原料气体进料管贯穿所述原料气体进口并与所述气体分布搅拌部件连通。
优选地，当所述循环流体进料管为一个时，所述循环流体进料管与反应釜中心轴之间的垂直距离为0～3*D/8，D为反应釜直径；当所述循环流体进料管为二个以上时，相邻循环流体进料管的中心轴在反应釜的径向平面上的垂直投影的夹角为60°～150°，如60°～120°或 120°～150°。
优选地，所述气体分布搅拌单元包括如下技术特征中的至少一项：
a)所述气体分布搅拌单元呈圆环状，沿反应釜中心轴对称布置；
b)当所述气体分布搅拌单元为二个以上时，二个以上所述气体分布搅拌单元沿反应釜中心轴多层分布且连通，从近原料气体进口端的底层气体分布搅拌单元至远原料气体进口端的顶层气体分布搅拌单元，各层气体分布搅拌单元的直径依次增加；
c)所述气体分布搅拌单元的直径计算公式如下：
Dn i＝D*n i/(n+1)；
其中，D为反应釜的直径，Dn i为第n i层气体分布搅拌单元的外圆直径；n i＝1，所述气体分布搅拌单元为最接近原料气体进口端；n i为从最接近原料气体进口端的气体分布搅拌单元开始计所在的层数；n为气体分布搅拌部件的总层数。
更优选地，相邻气体分布搅拌单元的间距总和+底层气体分布搅拌单元与反应釜底部的间距≤反应釜的半径。
更优选地，从近原料气体进口端的底层气体分布搅拌单元至远原料气体进口端的顶层气体分布搅拌单元，各层气体分布搅拌单元依次连通。
相邻气体分布搅拌单元的高度总和≤反应釜的直径。
优选地，还包括如下技术特征中的至少一项：
1)所述气体分布搅拌单元上设有均匀对称或交错分布的气孔；
2)所述反应釜还设有反应液出口，用于输出反应液；
3)设于所述反应釜内的循环流体进料管的端部设有喷头；
4)所述原料气体进口设于所述反应釜底部；
5)所述循环流体出口设于所述反应釜中部；
6)所述循环流体进口设于所述反应釜顶部；
7)所述循环流体搅拌部件还包括循环流体泵和/或循环流体换热器，所述循环流体出口经所述循环流体泵和/或所述循环流体换热器分至少一个通路分别与所述至少一个循环流体进料管连接；
8)所述原料气体分布搅拌部件设于所述反应釜底部。
更优选地，还包括如下技术特征中的至少一项：
11)特征1)中，气孔直径为2mm～10mm，如2mm～6mm、6mm～7mm或7mm～10mm；
12)特征1)中，气孔间距为20mm～60mm；
31)特征3)中，所述喷头位于所述反应釜内中部；
32)特征3)中，所述喷头为缩径结构；
33)特征3)中，所述喷头位于反应装置液位以下1/6H～1/2H，如1/6H～2/6H、2/6H～2/5H、2/5H～1/2H，其中，H为反应釜的筒体直边长度；
71)特征7)中，所述循环流体搅拌部件包括至少一个循环流体泵和/或至少一个循环流体换热器，所述循环流体出口分至少一个通路分别与所述至少一个循环流体进料管连接，单个通路上设有一个循环流体泵和/或一个循环流体换热器。
本发明第二方面提供一种羰基合成醋酸的系统，包括依次连通的上述反应装置、闪蒸分离器和精制单元。
优选地，所述闪蒸分离器设有气相出口和液相出口，气相出口与所述精制单元连通，液相出口与所述反应装置连通。
本发明第三方面提供一种羰基合成醋酸的方法，采用上述反应装置，将包括甲醇、CO和催化剂的反应原料通入所述反应装置，采用所述循环流体搅拌部件和所述气体分布搅拌部件和对物料进行搅拌，在催化剂的作用下反应生成醋酸。
优选地，还包括如下技术特征中的至少一项：
1)还包括如下步骤：反应液经闪蒸分离，分别得到气相物料和液相物料；气相物料精制得到醋酸产品，液相物料回流至所述反应装置；
2)气体分布搅拌单元的气孔出口流速为5m/s～30m/s，如5m/s～7m/s、7m/s～15m/s、15m/s～20m/s、20m/s～25m/s或25m/s～30m/s；
3)循环流体进料管的喷头喷出的流体流速为5m/s～20m/s，如5m/s～11m/s、11m/s～15m/s或15m/s～20m/s；循环流体从循环流体进料管端部的喷头以较高的速度喷出，带动周边的液体发生矢量的改变，并从反应釜底部翻转而上，对反应釜内液体产生更大的扰动，在反应釜内形成多个大的循环流动状态，确保整个反应釜内液体混合均匀，从而实现反应釜内液体的浓度场分布和温度场分布均匀；
4)两个以上循环流体进料管出口每小时总流体流量为反应液体积的5倍～10倍，如5倍～6.2倍、6.2倍～7.5倍或7.5倍～10倍。
本发明的有益效果为：
本发明反应装置包括循环流体搅拌部件和原料气体分布搅拌部件，用于甲醇低压羰基合成醋酸生产中，整个反应装置中没有动密封点，消除机械搅拌可能因机封泄漏造成的停车隐患以及釜内搅拌部件因腐蚀导致失效需更换，保障反应系统安全稳定运行，而且节约投资、 运行、维护费用的支出；立体多层环式的原料气体分布搅拌部件使反应釜内的气体分布更加均匀，改善气液两相混合效果，优化系统内部反应状态，反应釜内温差减小，副反应减少；配置的流体循环搅拌系统使液体分布更加均匀，反应釜内温度场更加均匀，保证生产更加稳定，产能得到提升。
附图说明
图1为本发明反应装置的结构示意图一。
图2为本发明反应装置的结构示意图二。
图3为本发明循环流体搅拌部件中两个循环流体进料管的俯视结构示意图。
图4为本发明气体分布搅拌部件的俯视结构示意图。
图5为羰基合成醋酸的系统图。
图6为本发明循环流体搅拌部件中单个循环流体进料管的侧视结构示意图。
附图标记
1                      反应装置
11                     反应釜
1111                   原料气体进料管
1112                   原料气体进口
1121                   循环流体出口
1122                   循环流体进口
12                     循环流体搅拌部件
121                    循环流体进料管
1211                   喷头
122                    循环流体泵
123                    循环流体换热器
13                     原料气体分布搅拌部件
131                    气体分布搅拌单元
1311                   气孔
2                      闪蒸分离器
21                     气相出口
22                     液相出口
3                      精制单元
具体实施方式
以下通过特定的具体实例说明本发明的技术方案。应理解，本发明提到的一个或多个方法步骤并不排斥在所述组合步骤前后还存在其他方法步骤或在这些明确提到的步骤之间还可以插入其他方法步骤；还应理解，这些实施例仅用于说明本发明而不用于限制本发明的范围。而且，除非另有说明，各方法步骤的编号仅为鉴别各方法步骤的便利工具，而非为限制各方法步骤的排列次序或限定本发明可实施的范围，其相对关系的改变或调整，在无实质变更技术内容的情况下，当亦视为本发明可实施的范畴。
一种反应装置，如图1和图2所示，包括反应釜11、循环流体搅拌部件12和原料气体分布搅拌部件13；所述反应釜11包括原料气体进料管1111，所述反应釜11设有原料气体进口1112、循环流体出口1121、至少一个循环流体进口1122；所述循环流体搅拌部件12包括至少一个循环流体进料管121；所述气体分布搅拌部件13设于所述反应釜11内，所述气体分布搅拌部件13包括至少一个气体分布搅拌单元131；所述循环流体进料管121贯穿所述循环流体进口1122并与所述循环流体出口1121连通；所述原料气体进料管1111贯穿所述原料气体进口1112并与所述气体分布搅拌部件13连通。
使用立体多层的气体分布搅拌部件，便于CO气体在反应釜11截面上均匀分布，CO气体从不同高度的气孔出来后向上运动，减少CO气泡聚并现象，使整个反应釜11内CO气体以较小的气泡形式存在，减少CO向液体中的扩散阻力，确保反应釜11内气体分布比较均匀，改善气液两相的混合效果。
在一个优选的实施例中，当循环流体进料管121为一个时，如图6所示，循环流体进料管121与反应釜中心轴之间的垂直距离为0～3*D/8，D为反应釜直径。1个循环流体进料管液体的均匀性好，这样温度场和浓度场更加均匀，副反应少，产能也可以高一些。
在一个优选的实施例中，当循环流体进料管121为二个以上时，相邻循环流体进料管121的中心轴在反应釜的径向平面上的垂直投影的夹角为60°～150°，该夹角即为见图3中α。该设计确保反应釜中液体均匀性比较好，反应釜中反应比较均匀，温差减小，副反应减少。
在一个优选的实施例中，如图1和图4所示，气体分布搅拌单元131呈圆环状，沿反应釜中心轴对称布置。
在一个优选的实施例中，如图1和图4所示，当气体分布搅拌单元131为二个以上时， 二个以上气体分布搅拌单元131沿反应釜中心轴多层分布且连通，从近原料气体进口端的底层气体分布搅拌单元至远原料气体进口端的顶层气体分布搅拌单元，各层气体分布搅拌单元131的直径依次增加。
在一个优选的实施例中，如图1和图4所示，所述气体分布搅拌单元131的直径计算公式如下：
Dn i＝D*n i/(n+1)；
其中，D为反应釜的直径，Dn i为第n i层气体分布搅拌单元的外圆直径；n i＝1，所述气体分布搅拌单元为最接近原料气体进口端；n i为从最接近原料气体进口端的气体分布搅拌单元开始计所在的层数；n为气体分布搅拌部件的总层数。该设计确保气体分布均匀，反应釜中反应比较均匀，温差减小，副反应减少。
如图1和图4所示，所述气体分布搅拌部件13为多层圆环式管体相互连通结构，自下而上第一层圆环外圆直径D1、第二层圆环外圆直径D2、第三层圆环外圆直径D3依次增加至Dn，D1＝D*1/(n+1)，D2＝D*2/(n+1)，依此类推，其中D为反应釜的直径，n为气体分布搅拌部件的总层数。
在一个优选的实施例中，相邻气体分布搅拌单元的间距总和+底层气体分布搅拌单元与反应釜底部的间距≤反应釜的半径。例如：反应釜底部与底层气体分布搅拌单元即第一层圆环之间高度为H1，底层气体分布搅拌单元即第一层圆环与第二层圆环之间高度为H2，第二层圆环与第三层圆环之间高度为H3，依次第n-1层圆环与第n层圆环之间高度为Hn，且H1+H2+H3+...Hn≤反应釜的半径。该设计确保气体分布均匀，反应釜中反应比较均匀，温差减小，副反应减少。
在一个优选的实施例中，从近原料气体进口端的底层气体分布搅拌单元至远原料气体进口端的顶层气体分布搅拌单元，各层气体分布搅拌单元131依次连通。上述设置时，所述循环流体进料管121为二个以上。
在一个优选的实施例中，所述气体分布搅拌单元131上设有均匀对称或交错分布的气孔1311。
在一个优选的实施例中，气孔直径为2mm～10mm，如2mm～6mm、6mm～7mm或7mm～10mm。
在一个优选的实施例中，气孔间距为20mm～60mm。
在一个优选的实施例中，所述反应釜11还设有反应液出口，用于输出反应液。
在一个优选的实施例中，设于所述反应釜11内的循环流体进料管121的端部设有喷头 1211。
在一个优选的实施例中，所述喷头1211位于所述反应釜11内中部。
在一个优选的实施例中，所述喷头1211为缩径结构。该设计可以保证喷头出口处的液体以较高的速度喷涌而出。
在一个优选的实施例中，所述喷头1211位于反应装置液位以下1/6H～1/2H，如1/6H～2/6H、2/6H～2/5H、2/5H～1/2H，其中，H为反应釜的筒体直边长度。该设计使得液体混合更加均匀，反应釜中反应比较均匀，温差减小，副反应减少。
在一个优选的实施例中，所述原料气体进口1112设于所述反应釜11底部。
在一个优选的实施例中，所述循环流体出口1121设于所述反应釜11中部。
在一个优选的实施例中，所述循环流体进口1122设于所述反应釜11顶部。
在一个优选的实施例中，所述循环流体搅拌部件12还包括循环流体泵122和/或循环流体换热器123，所述循环流体出口1121经所述循环流体泵122和/或所述循环流体换热器123分至少一个通路分别与所述至少一个循环流体进料管121连接。如图1所示，循环流体出口连接一台循环流体泵122，经一台循环流体换热器123冷却后，分成至少一股分别经至少一个循环流体进料管121进入反应釜内，从端部的喷头以较高的速度喷出，实现对反应釜内液体的均匀搅拌混合。
在一个优选的实施例中，所述循环流体搅拌部件12包括至少一个循环流体泵122和/或至少一个循环流体换热器123，所述循环流体出口1121分至少一个通路分别与所述至少一个循环流体进料管121连接，单个通路上设有一个循环流体泵122和/或一个循环流体换热器123。其中，如图2所示，循环流体出口分成两股，分别连接一台循环流体泵122，分别经循环流体换热器123冷却后，分别经两个循环流体进料管121进入反应釜内，从端部的喷头以较高的速度喷出，实现对反应釜内液体的均匀搅拌混合，尤其适用于返料量较大的反应装置，以达到运行稳定，反应釜内液体均匀混合的效果。如图6所示，循环流体出口为一股，连接一台循环流体泵122，经一个循环流体换热器123冷却后，经一个循环流体进料管121进入反应釜内，从端部的喷头以较高的速度喷出，实现对反应釜内液体的均匀搅拌混合。
在一个优选的实施例中，所述原料气体分布搅拌部件13设于所述反应釜11底部。
本发明第二方面提供一种羰基合成醋酸的系统，如图5所示，包括依次连通的上述反应装置1、闪蒸分离器2和精制单元3。
在一个优选的实施例中，所述闪蒸分离器2设有气相出口21和液相出口22，气相出口21与所述精制单元3连通，液相出口22与所述反应装置1连通。
下述实施例1至3采用一种优选的反应装置，如图1、图3和图4所示，包括反应釜11、循环流体搅拌部件12和原料气体分布搅拌部件13；所述反应釜11包括原料气体进料管1111，所述反应釜11设有原料气体进口1112、循环流体出口1121、至少一个循环流体进口1122；所述循环流体搅拌部件12包括至少一个循环流体进料管121；所述气体分布搅拌部件13设于所述反应釜11内，所述气体分布搅拌部件13包括至少一个气体分布搅拌单元131；所述循环流体进料管121贯穿所述循环流体进口1122并与所述循环流体出口1121连通；所述原料气体进料管1111贯穿所述原料气体进口1112并与所述气体分布搅拌部件13连通。
气体分布搅拌单元131呈圆环状，沿反应釜中心轴对称布置；当所述气体分布搅拌单元131为二个以上时，二个以上所述气体分布搅拌单元131沿反应釜中心轴多层分布且连通，从近原料气体进口端的底层气体分布搅拌单元至远原料气体进口端的顶层气体分布搅拌单元，各层气体分布搅拌单元131的直径依次增加，所述气体分布搅拌单元131的直径计算公式如下：
Dn i＝D*n i/(n+1)；
其中，D为反应釜的直径，Dn i为第n i层气体分布搅拌单元的外圆直径；n i＝1，所述气体分布搅拌单元为最接近原料气体进口端；n i为从最接近原料气体进口端的气体分布搅拌单元开始计所在的层数；n为气体分布搅拌部件的总层数。从近原料气体进口端的底层气体分布搅拌单元至远原料气体进口端的顶层气体分布搅拌单元，各层气体分布搅拌单元131依次连通。所述反应釜11还设有反应液出口，用于输出反应液。设于所述反应釜11内的循环流体进料管121的端部设有喷头1211。所述喷头1211位于所述反应釜11内中部。所述喷头1211为缩径结构。所述喷头1211位于反应装置液位以下1/6H～1/2H，其中，H为反应釜的筒体直边长度。所述原料气体进口1112设于所述反应釜11底部。所述循环流体出口1121设于所述反应釜11中部。所述循环流体进口1122设于所述反应釜11顶部。所述循环流体搅拌部件12还包括循环流体泵122和循环流体换热器123，所述循环流体出口1121经所述循环流体泵122和所述循环流体换热器123分至少一个通路分别与所述至少一个循环流体进料管121连接。所述原料气体分布搅拌部件13设于所述反应釜11底部。
对比例
甲醇低压合成醋酸工业装置，反应釜改造前采用机械搅拌装置，反应釜筒体高度为5m，直径为3m，单层管体CO分布器，外圆直径为2m，CO分布器上设有均匀对称的气孔，气孔直径为15mm，外圆直径为1m，循环流体进料管(一根)的出口位于液面以上且无缩径。在一 定温度和压力、且催化剂存在条件下，甲醇与CO发生羰基化反应生成醋酸，反应釜轴向温差约3℃。
实施例1
甲醇低压合成醋酸反应装置，反应釜筒体高度(即反应釜的筒体直边长度)为5m，直径为3m，反应釜改造后，采用图1、图3和图4所示的循环流体搅拌部件及立体多环的原料气体分布搅拌部件，两根循环流体进料的中心轴在反应釜的径向平面上的垂直投影的夹角为150°，两根循环流体进料管端部喷头位于液面以下5/6m处(为反应釜的筒体直边长度的1/6)，循环流体进料管的喷头喷出的流体流速为5m/s，循环流体进料管出口流体总流量为200m 3/h，为反应液体积的5倍。原料气体分布搅拌部件包括两个气体分布搅拌单元131即两层，外圆直径分别为1m和2m，气体分布搅拌单元上设有均匀对称的气孔，气孔直径为6mm，出气孔的平均气速为5m/s，相邻气体分布搅拌单元的间距总和+底层气体分布搅拌单元即第一层气体分布搅拌单元与反应釜底部的间距为1.2m。在与对比例相同的温度和压力、且催化剂存在条件下，甲醇与CO发生羰基化反应生成醋酸，反应釜轴向温度相对对比例减小2℃即反应釜轴向温差约1℃，产品中丙酸含量降低100ppm。
实施例2
甲醇低压合成醋酸反应装置，反应釜筒体高度为5m，直径为3m，反应釜改造后，采用图2、图3和图4所示的循环流体搅拌部件及立体多环的原料气体分布搅拌部件，3根循环流体进料管，相邻循环流体进料管121的中心轴在反应釜的径向平面上的垂直投影的夹角为120°，循环流体进料管端部喷头位于液面以下10/6m处(为反应釜的筒体直边长度的2/6)，循环流体进料管的喷头喷出的流体流速为11m/s，循环流体进料管出口流体总流量为260m 3/h，为反应液体积的6.2倍。原料气体分布搅拌部件包括三个气体分布搅拌单元131即三层，外圆直径分别为0.75m、1.5m和2.25m，气体分布搅拌单元上设有均匀对称的气孔，气孔直径为10mm，出气孔的平均气速为15m/s，相邻气体分布搅拌单元的间距总和+底层气体分布搅拌单元即第一层气体分布搅拌单元与反应釜底部的间距为1.0m。在与对比例相同的温度和压力、且催化剂存在条件下，甲醇与CO发生羰基化反应生成醋酸，反应釜轴向温度相对对比例减小1℃即反应釜轴向温差约2℃，产品中丙酸含量降低70ppm。
实施例3
甲醇低压合成醋酸反应装置，反应釜筒体高度为5m，直径为3m，反应釜改造后，采用图2、图3和图4所示的循环流体搅拌部件及立体多环的原料气体分布搅拌部件，四根循环流体进料管，相邻循环流体进料管121的中心轴在反应釜的径向平面上的垂直投影的夹角为60°，循环流体进料管端部喷头位于液面以下15/6m处(为反应釜的筒体直边长度的1/2)，循环流体进料管的喷头喷出的流体流速为15m/s，循环流体进料管出口流体总流量为320m 3/h，为反应液体积的7.5倍，原料气体分布搅拌部件包括四个气体分布搅拌单元131即四层，外圆直径分别为0.6m，1.2m，1.8m，2.4m，气体分布搅拌单元上设有均匀对称的气孔，气孔直径为2mm，出气孔的平均气速为20m/s，相邻气体分布搅拌单元的间距总和+底层气体分布搅拌单元即第一层气体分布搅拌单元与反应釜底部的间距为1.2m。在与对比例相同的温度和压力、且催化剂存在条件下，甲醇与CO发生羰基化反应生成醋酸，反应釜轴向温度相对对比例减小0.5℃即反应釜轴向温差约2.5℃，产品中丙酸含量降低80ppm。
实施例4
甲醇低压合成醋酸反应装置，反应釜筒体高度为5m，直径为3m，反应釜改造后，采用图2、图3和图4所示的循环流体搅拌部件及立体多环的原料气体分布搅拌部件，两根循环流体进料管的中心轴在反应釜的径向平面上的垂直投影的夹角为120°，两根循环流体进料管端部喷头位于液面以下12/6处(为反应釜的筒体直边长度的2/5)，循环流体进料管的喷头喷出的流体流速为20m/s，循环流体进料管出口流体总流量为423m 3/h，为反应液体积的10倍，原料气体分布搅拌部件包括五个气体分布搅拌单元131即五层，外圆直径分别为0.5m，1m，1.5m，2m，2.5m，气体分布搅拌单元上设有均匀对称的气孔，气孔直径为7mm，出气孔的平均气速为30m/s，相邻气体分布搅拌单元的间距总和+底层气体分布搅拌单元即第一层气体分布搅拌单元与反应釜底部的间距为1.4m。在与对比例相同的温度和压力、且催化剂存在条件下，甲醇与CO发生羰基化反应生成醋酸，反应釜轴向温度相对对比例减小2.5℃即反应釜轴向温差约0.5℃，产品中丙酸含量降低120ppm。
以上所述，仅为本发明的较佳实施例，并非对本发明任何形式上和实质上的限制，应当指出，对于本技术领域的普通技术人员，在不脱离本发明方法的前提下，还将可以做出若干改进和补充，这些改进和补充也应视为本发明的保护范围。凡熟悉本专业的技术人员，在不脱离本发明的精神和范围的情况下，当可利用以上所揭示的技术内容而做出的些许更动、修饰与演变的等同变化，均为本发明的等效实施例；同时，凡依据本发明的实质技术对上述实 施例所作的任何等同变化的更动、修饰与演变，均仍属于本发明的技术方案的范围内。

Claims (10)

  1. 一种反应装置，其特征在于，包括反应釜(11)、循环流体搅拌部件(12)和原料气体分布搅拌部件(13)；所述反应釜(11)包括原料气体进料管(1111)，所述反应釜(11)设有原料气体进口(1112)、循环流体出口(1121)、至少一个循环流体进口(1122)；所述循环流体搅拌部件(12)包括至少一个循环流体进料管(121)；所述气体分布搅拌部件(13)设于所述反应釜(11)内，所述气体分布搅拌部件(13)包括至少一个气体分布搅拌单元(131)；所述循环流体进料管(121)贯穿所述循环流体进口(1122)并与所述循环流体出口(1121)连通；所述原料气体进料管(1111)贯穿所述原料气体进口(1112)并与所述气体分布搅拌部件(13)连通。
  2. 如权利要求1所述的反应装置，其特征在于，当所述循环流体进料管(121)为一个时，所述循环流体进料管(121)与反应釜中心轴之间的垂直距离为0～3*D/8，D为反应釜(11)直径；当所述循环流体进料管(121)为二个以上时，相邻循环流体进料管(121)的中心轴在反应釜(11)的径向平面上的垂直投影的夹角为60°～150°。
  3. 如权利要求1所述的反应装置，其特征在于，所述气体分布搅拌单元(131)包括如下技术特征中的至少一项：
    a)所述气体分布搅拌单元(131)呈圆环状，沿反应釜中心轴对称布置；
    b)当所述气体分布搅拌单元(131)为二个以上时，二个以上所述气体分布搅拌单元(131)沿反应釜中心轴多层分布且连通，从近原料气体进口端的底层气体分布搅拌单元至远原料气体进口端的顶层气体分布搅拌单元，各层气体分布搅拌单元(131)的直径依次增加；
    c)所述气体分布搅拌单元(131)的直径计算公式如下：
    Dn i＝D*n i/(n+1)；
    其中，D为反应釜的直径，Dn i为第n i层气体分布搅拌单元的外圆直径；n i＝1，所述气体分布搅拌单元为最接近原料气体进口端；n i为从最接近原料气体进口端的气体分布搅拌单元开始计所在的层数；n为气体分布搅拌部件的总层数。
  4. 如权利要求3所述的反应装置，其特征在于，相邻气体分布搅拌单元的间距总和+底层气体分布搅拌单元与反应釜底部的间距≤反应釜的半径。
  5. 如权利要求1所述的反应装置，其特征在于，还包括如下技术特征中的至少一项：
    1)所述气体分布搅拌单元(131)上设有均匀对称或交错分布的气孔(1311)，；
    2)所述反应釜(11)还设有反应液出口，用于输出反应液；
    3)设于所述反应釜(11)内的循环流体进料管(121)的下端部设有喷头(1211)；
    4)所述原料气体进口(1112)设于所述反应釜(11)底部；
    5)所述循环流体出口(1121)设于所述反应釜(11)中部；
    6)所述循环流体进口(1122)设于所述反应釜(11)顶部；
    7)所述循环流体搅拌部件(12)还包括循环流体泵(122)和/或循环流体换热器(123)，所述循环流体出口(1121)经所述循环流体泵(122)和/或所述循环流体换热器(123)分至少一个通路分别与所述至少一个循环流体进料管(121)连接；
    8)所述原料气体分布搅拌部件(13)设于所述反应釜(11)底部。
  6. 如权利要5所述的反应装置，其特征在于，还包括如下技术特征中的至少一项：
    11)特征1)中，气孔直径为2mm～10mm；
    12)特征1)中，气孔间距为20mm～60mm；
    31)特征3)中，所述喷头(1211)位于所述反应釜(11)内中部；
    32)特征3)中，所述喷头(1211)为缩径结构；
    33)特征3)中，所述喷头(1211)位于反应装置液位以下1/6H～1/2H，其中，H为反应釜的筒体直边长度；
    71)特征7)中，所述循环流体搅拌部件(12)包括至少一个循环流体泵(122)和/或至少一个循环流体换热器(123)，所述循环流体出口(1121)分至少一个通路分别与所述至少一个循环流体进料管(121)连接，单个通路上设有一个循环流体泵(122)和/或一个循环流体换热器(123)。
  7. 一种羰基合成醋酸的系统，其特征在于，包括依次连通的权利要求1至6任一项所述的反应装置(1)、闪蒸分离器(2)和精制单元(3)。
  8. 如权利要求7所述的羰基合成醋酸的系统，其特征在于，所述闪蒸分离器(2)设有气相出口(21)和液相出口(22)，气相出口(21)与所述精制单元(3)连通，液相出口(22)与所述反应装置(1)连通。
  9. 一种羰基合成醋酸的方法，其特征在于，采用权利要求1至6任一项所述的反应装置，将包括甲醇、CO和催化剂的反应原料通入所述反应装置，采用所述循环流体搅拌部件和所述气体分布搅拌部件和对物料进行搅拌，在催化剂的作用下反应生成醋酸。
  10. 如权利要求9所述的羰基合成醋酸的方法，其特征在于，还包括如下技术特征中的至少一项：
    1)还包括如下步骤：反应液经闪蒸分离，分别得到气相物料和液相物料；气相物料精制得到醋酸产品，液相物料回流至所述反应装置；
    2)气体分布搅拌单元的气孔出口流速为5m/s～30m/s；
    3)循环流体进料管的喷头喷出的流体流速为5m/s～20m/s；
    4)两个以上循环流体进料管出口每小时总流体流量为反应液体积的5倍～10倍。
PCT/CN2021/132466 2021-01-06 2021-11-23 一种反应装置及羰基合成醋酸的系统和方法 WO2022148162A1 (zh)

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