WO2021189639A1 - 一种离子液体催化丙烯水合的强化反应系统及工艺 - Google Patents

一种离子液体催化丙烯水合的强化反应系统及工艺 Download PDF

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WO2021189639A1
WO2021189639A1 PCT/CN2020/092758 CN2020092758W WO2021189639A1 WO 2021189639 A1 WO2021189639 A1 WO 2021189639A1 CN 2020092758 W CN2020092758 W CN 2020092758W WO 2021189639 A1 WO2021189639 A1 WO 2021189639A1
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propylene
gas
reactor
liquid
micro
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PCT/CN2020/092758
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English (en)
French (fr)
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张志炳
周政
张锋
李磊
孟为民
王宝荣
杨高东
罗华勋
杨国强
田洪舟
曹宇
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南京延长反应技术研究院有限公司
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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
    • B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
    • B01J10/002—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor carried out in foam, aerosol or bubbles
    • 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
    • B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions

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  • the invention relates to the technical field of isopropanol preparation, in particular to an enhanced reaction system and process for ionic liquid to catalyze the hydration of propylene.
  • Propylene can be used as raw material to produce isopropanol through hydration reaction.
  • Propylene is a colorless, slightly sweet gas, flammable at room temperature, and has an explosion limit of 2% to 11%. It is insoluble in water, soluble in ethanol, Organic solvents such as ether have low toxicity.
  • Propylene gas phase direct hydration method is divided into gas phase direct hydration method to prepare isopropanol and liquid phase direct hydration method to prepare isopropanol.
  • Liquid phase direct hydration method is a kind of tungsten heteropoly acid with good activity, stability and selectivity.
  • a method in which the catalyst catalyzes the direct hydration reaction of propylene The reaction raw material propylene is preheated by a heating device and passed into the reactor. The catalyst is dissolved in the process reaction water and enters the reactor. The reaction temperature of this method is 240 ⁇ 280°C and the pressure is 20Mpa. Propanol exists in the solution, and the aqueous solution of the catalyst tungsten polyanion has higher activity and life, and a higher single-pass conversion rate of propylene can be obtained.
  • this method has obvious shortcomings and shortcomings in the use process:
  • the present invention provides an enhanced reaction system and process for the hydration of propylene catalyzed by an ionic liquid, so as to reduce the preset conditions for preparing isopropanol by the liquid-phase direct hydration method in the prior art.
  • the present invention provides an enhanced reaction system for ionic liquid catalyzed hydration of propylene, including:
  • the reactor is used to provide a reaction place for deionized water, catalyst and propylene to prepare isopropanol;
  • the micro-interface generator converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubble and transmits it to the gas reactant, and breaks the gas reactant propylene to form micron-sized bubbles with a diameter of ⁇ 1 ⁇ m and ⁇ 1mm to improve The mass transfer area between the gas reactant and the liquid reactant, reduces the thickness of the liquid film, and reduces the mass transfer resistance;
  • a preheating device which is connected to the micro-interface generator, and is used to preheat the propylene entering the micro-interface generator;
  • a gas-liquid separator which is connected to the reactor, and is used to separate the product once;
  • An azeotropic tower which is connected to the gas-liquid separator, is used to perform secondary separation treatment on the product.
  • the micro-interface generator is a pneumatic micro-interface generator, the micro-interface generator is located inside the reactor, and the micro-interface generator is used to break the propylene into micro-scale bubbles of micron scale and complete the crushing. Then, the micron-sized bubbles are output into the reactor and mixed with the ionic liquid catalyst in the reactor to form a gas-liquid emulsion.
  • the preheating device is provided with a circulating preheating pipe, and the preheating device has a preheating effect on propylene by passing hot fluid into the circulating preheating pipe, and one side of the preheating device is provided There is a first pump body and a heat exchanger, and the hot fluid is circulated in the circulating preheating pipe through the first pump body, and the temperature of the hot fluid is maintained by the heat exchanger.
  • micro-interface generator is connected with a propylene transfer tube, and a second pump body is arranged between the propylene transfer tube and the preheating device, and the preheated propylene is heated by the second pump body. It is transferred to the micro-interface generator along the propylene transfer pipe.
  • the reactor is provided with a deionized water inlet pipe and a catalyst inlet pipe in communication, and the deionized water inlet pipe and the catalyst inlet pipe are used for supplying the deionized water and the catalyst to enter the reactor.
  • the reactor and the gas-liquid separator are connected through a material transfer pipe, and a third pump body is installed on the material transfer pipe.
  • the product of the product is transferred to the gas-liquid separator along the material transfer pipe.
  • a fourth pump body is arranged between the gas-liquid separator and the preheating device, and the gas-phase propylene in the gas-liquid separator is transferred back to the preheating device through the fourth pump body.
  • a fifth pump body is arranged between the gas-liquid separator and the azeotropic tower, and the liquid phase product in the gas-liquid separator is transferred to the azeotropic tower through the fifth pump body.
  • a sixth pump body is arranged between the azeotropic tower and the reactor, and the liquid containing the catalyst at the bottom of the azeotrope tower is transferred back to the reactor for repeated use through the sixth pump body.
  • the present invention provides an enhanced reaction process for ionic liquid catalyzed hydration of propylene, which includes:
  • Step 1 Add deionized water and catalyst into the reactor through the deionized water inlet pipe and the catalyst inlet pipe, and mix them uniformly to form an ionic liquid catalyst;
  • Step 2 Pass the hot fluid into the circulating preheating tube through the first pump body to circulate, maintain the temperature of the hot fluid through the work of the heat exchanger, and pass propylene into the preheating device, and the hot fluid makes the
  • the preheating device has a preheating effect on propylene, and the preheated propylene is transferred to the micro-interface generator along the propylene transfer pipe through the operation of the second pump body;
  • Step 3 The micro-interface generator works to break propylene into micron-sized micro-sized bubbles, and after the crushing is completed, the micro-sized bubbles are output into the reactor and mixed with the ionic liquid catalyst in the reactor to form a gas-liquid Emulsion, propylene hydrates;
  • Step 4 Through the operation of the third pump body, the product generated in the reactor is transferred to the gas-liquid separator along the material transfer pipe, and the product is condensed and separated into unreacted in the gas-liquid separator
  • the gas-phase propylene and liquid-phase product of the gas-phase propylene in the gas-liquid separator are transferred back to the preheating device through the work of the fourth pump body, and then used as raw materials to participate in the reaction again.
  • the liquid phase products in the gas-liquid separator are transferred to the azeotropic tower;
  • Step 5 The liquid phase product is separated and concentrated in the azeotropic tower, the isopropanol solution is obtained at the top of the tower, the solution containing the catalyst is obtained at the bottom of the tower, and the bottom of the azeotropic tower contains The catalyst liquid is transported back to the reactor for reuse.
  • the temperature in the reactor is 200-220°C
  • the pressure is 14-16Mpa.
  • the beneficial effect of the present invention is that the present invention breaks the propylene gas to form micro-scale micro-sized bubbles, which have physical and chemical properties that conventional bubbles do not have.
  • the volume and surface area of the sphere are calculated The formula shows that when the total volume is constant, the total surface area of the bubbles is inversely proportional to the diameter of a single bubble. It can be seen that the total surface area of the micron-sized bubbles is huge, and the micron-sized bubbles are mixed with the ionic liquid catalyst to form a gas-liquid emulsion. Increase the contact area of the gas-liquid two-phase, and achieve the effect of enhancing mass transfer within the lower preset operating conditions, and at the same time further increase the conversion rate of propylene to a certain extent;
  • the reactor is used to provide a reaction place for deionized water, catalyst and propylene to prepare isopropanol;
  • the micro-interface generator converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubble and transmits it to the gas reactant, and breaks the gas reactant propylene to form micron-sized bubbles with a diameter of ⁇ 1 ⁇ m and ⁇ 1mm to improve The mass transfer area between the gas reactant and the liquid reactant, reduces the thickness of the liquid film, and reduces the mass transfer resistance;
  • a preheating device which is connected to the micro-interface generator, and is used to preheat the propylene entering the micro-interface generator;
  • a gas-liquid separator which is connected to the reactor, and is used to separate the product once;
  • An azeotropic tower which is connected to the gas-liquid separator, is used to perform secondary separation treatment on the product.
  • the micro-interface generator is a pneumatic micro-interface generator, the micro-interface generator is located inside the reactor, and the micro-interface generator is used to break the propylene into micro-scale bubbles of micron scale and complete the crushing. Then, the micron-sized bubbles are output into the reactor and mixed with the ionic liquid catalyst in the reactor to form a gas-liquid emulsion.
  • the preheating device is provided with a circulating preheating pipe, and the preheating device has a preheating effect on propylene by passing hot fluid into the circulating preheating pipe, and one side of the preheating device is provided There is a first pump body and a heat exchanger, and the hot fluid is circulated in the circulating preheating pipe through the first pump body, and the temperature of the hot fluid is maintained by the heat exchanger.
  • the micro-interface generator is connected with a propylene transfer tube, and a second pump body is arranged between the propylene transfer tube and the preheating device, and the preheated propylene is heated by the second pump body. It is transferred to the micro-interface generator along the propylene transfer pipe.
  • the hot fluid is passed into the circulation preheating tube to circulate, the temperature of the hot fluid is maintained through the operation of the heat exchanger, and propylene is introduced into the preheating device, and the hot fluid makes the preheating device It has a preheating effect on propylene, and transmits the preheated propylene to the micro-interface generator along the propylene transfer pipe through the operation of the second pump body;
  • the reactor is connected with a deionized water inlet pipe and a catalyst inlet pipe, and the deionized water inlet pipe and the catalyst inlet pipe are used for supplying the deionized water and the catalyst to enter the reactor.
  • the reactor and the gas-liquid separator are connected through a material transfer pipe, and a third pump body is installed on the material transfer pipe.
  • the product of is transferred to the gas-liquid separator along the material transfer pipe;
  • a fourth pump body is arranged between the gas-liquid separator and the preheating device, and the gas-phase propylene in the gas-liquid separator is transferred back to the preheating device through the fourth pump body.
  • a fifth pump body is arranged between the gas-liquid separator and the azeotropic tower, and the liquid phase product in the gas-liquid separator is transferred to the azeotropic tower through the fifth pump body;
  • Three pumps work to transport the products generated in the reactor along the material transfer pipe to the gas-liquid separator, and the products are condensed and separated into unreacted gas-phase propylene and liquid-phase products in the gas-liquid separator ,
  • the gas-phase propylene in the gas-liquid separator is transferred back to the preheating device through the work of the fourth pump body, and is used as a raw material to participate in the reaction again, and the liquid in the gas-liquid separator is reduced by the work of the fifth pump body.
  • the phase product is transferred to the azeotropic tower;
  • a sixth pump body is arranged between the azeotropic tower and the reactor, and the liquid containing the catalyst at the bottom of the azeotrope tower is transferred back to the reactor for repeated use through the sixth pump body.
  • the liquid phase product is separated and concentrated in the azeotropic tower, the isopropanol solution is obtained at the top of the tower, the solution containing the catalyst is obtained at the bottom of the tower, and the catalyst-containing liquid at the bottom of the azeotrope Transfer back to the reactor for reuse.
  • Fig. 1 is a structural schematic diagram of an enhanced reaction system for catalyzing hydration of propylene with an ionic liquid according to the present invention.
  • the terms “installed”, “connected”, and “connected” should be understood in a broad sense. For example, they can be fixed or fixed. It is a detachable connection or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the internal communication between two components.
  • installed e.g., they can be fixed or fixed. It is a detachable connection or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the internal communication between two components.
  • the specific meaning of the above-mentioned terms in the present invention can be understood according to specific circumstances.
  • FIG. 1 provides an enhanced reaction system for ionic liquid catalyzed hydration of propylene according to the present invention, including:
  • Reactor 1 is used to provide a reaction place for deionized water, catalyst and propylene to prepare isopropanol;
  • the micro-interface generator 2 which converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubble and transmits it to the gas reactant, and breaks the gas reactant propylene to form micron-sized bubbles with a diameter of ⁇ 1 ⁇ m and ⁇ 1mm. Increase the mass transfer area between the gas reactant and the liquid reactant, reduce the thickness of the liquid film, reduce the mass transfer resistance, and mix the liquid reactant with the micron-sized bubbles of the gas reactant to form a gas-liquid emulsion after being broken. Enhance the mass transfer efficiency and reaction efficiency between the liquid reactant and the gas reactant within the lower preset operating conditions;
  • a preheating device 3 which is connected to the micro-interface generator, and is used to preheat the propylene entering the micro-interface generator;
  • a gas-liquid separator 4 which is connected to the reactor, and is used to perform a primary separation treatment on the product
  • the azeotropic tower 5 is connected to the gas-liquid separator for secondary separation treatment of the product.
  • the micro-interface generator is a pneumatic micro-interface generator, the micro-interface generator is located inside the reactor, and the micro-interface generator is used to break propylene into micro-sized micro-sized bubbles and After the crushing is completed, the micron-sized bubbles are output into the reactor and mixed with the ionic liquid catalyst in the reactor to form a gas-liquid emulsion.
  • the preheating device is provided with a circulating preheating pipe 6, and the preheating device has a preheating effect on propylene by passing hot fluid into the circulating preheating pipe.
  • a first pump body 7 and a heat exchanger 8 are provided on one side of the, through which the thermal fluid is circulated in the circulating preheating tube, and the temperature of the thermal fluid is maintained by the heat exchanger.
  • the micro-interface generator is connected with a propylene transfer tube 9, and a second pump body 10 is provided between the propylene transfer tube and the preheating device.
  • the preheated propylene is transferred to the micro-interface generator along the propylene transfer pipe.
  • the reactor is provided with a deionized water inlet pipe 11 and a catalyst inlet pipe 12 in communication, and the deionized water inlet pipe and the catalyst inlet pipe are used for supplying deionized water and catalyst to enter the reaction. ⁇ In the device.
  • the reactor and the gas-liquid separator are connected through a material transfer pipe 13, and a third pump body 14 is installed on the material transfer pipe.
  • the products generated in the reactor are transferred to the gas-liquid separator along the material transfer pipe.
  • a fourth pump body is arranged between the gas-liquid separator and the preheating device, and the gas-phase propylene in the gas-liquid separator is transferred back to the preheating through the fourth pump body.
  • a fifth pump body 15 is arranged between the gas-liquid separator and the azeotropic tower 5, and the liquid phase product in the gas-liquid separator is transferred to the azeotropic tower through the fifth pump body .
  • a sixth pump body 16 is provided between the azeotrope tower 5 and the reactor, and the liquid containing the catalyst at the bottom of the azeotrope tower is transferred back to the reaction through the sixth pump body. Repeated use in the device.
  • the present invention provides an enhanced reaction process for ionic liquid catalyzed hydration of propylene, including:
  • Step 1 Add deionized water and catalyst into the reactor through the deionized water inlet pipe and the catalyst inlet pipe, and mix them uniformly to form an ionic liquid catalyst;
  • Step 2 Pass the hot fluid into the circulating preheating tube through the first pump body to circulate, maintain the temperature of the hot fluid through the work of the heat exchanger, pass propylene into the preheating device, and the hot fluid makes the
  • the preheating device has a preheating effect on propylene, and the preheated propylene is transferred to the micro-interface generator along the propylene transfer pipe through the operation of the second pump body;
  • Step 3 The micro-interface generator works to break propylene into micron-sized micro-sized bubbles, and after the crushing is completed, the micro-sized bubbles are output into the reactor and mixed with the ionic liquid catalyst in the reactor to form a gas-liquid Emulsion, propylene hydrates;
  • Step 4 Through the operation of the third pump body, the product generated in the reactor is transferred to the gas-liquid separator along the material transfer pipe, and the product is condensed and separated into unreacted in the gas-liquid separator
  • the gas-phase propylene and liquid-phase product of the gas-phase propylene in the gas-liquid separator are transferred back to the preheating device through the work of the fourth pump body, and then used as raw materials to participate in the reaction again.
  • the liquid phase products in the gas-liquid separator are transferred to the azeotropic tower;
  • Step 5 The liquid phase product is separated and concentrated in the azeotropic tower, the isopropanol solution is obtained at the top of the tower, the solution containing the catalyst is obtained at the bottom of the tower, and the bottom of the azeotropic tower 5 The liquid containing the catalyst is transported back to the reactor for reuse.
  • the temperature in the reactor is 200-220°C, and the pressure is 14-16Mpa.
  • the temperature of the reactor is 200°C, and the pressure inside the reactor is 14Mpa;
  • the gas-liquid ratio in the micro-interface generator is 900:1;
  • the temperature of the reactor is 205°C, and the pressure inside the reactor is 14Mpa;
  • the gas-liquid ratio in the micro-interface generator is 900:1;
  • the single-pass conversion rate of propylene is 80%.
  • the temperature of the reactor is 210°C, and the pressure inside the reactor is 15Mpa;
  • the gas-liquid ratio in the micro-interface generator is 900:1;
  • the single-pass conversion rate of propylene is 80%.
  • the temperature of the reactor is 215°C, and the pressure inside the reactor is 15Mpa;
  • the gas-liquid ratio in the micro-interface generator is 900:1;
  • the temperature of the reactor is 220°C, and the pressure inside the reactor is 16Mpa;
  • the gas-liquid ratio in the micro-interface generator is 900:1;
  • the prior art propylene direct hydration method is used to prepare isopropanol, wherein the temperature in the reactor is 240°C and the pressure is 20Mpa.

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Abstract

本发明涉及一种离子液体催化丙烯水合的强化反应系统及工艺，包括：反应器、微界面发生器和预热装置等。本发明通过破碎丙烯气体使其形成微米尺度的微米级气泡，微米级气泡具备常规气泡所不具备的理化性质，由球体体积及表面积的计算公式可知，在总体积不变的情况下，气泡的总表面积与单个气泡直径成反比，由此可知微米级气泡的总表面积巨大，使微米级气泡与离子液体催化剂混合形成气液乳化物，以增大气液两相的接触面积，并达到在较低预设操作条件范围内强化传质的效果，同时也在一定程度上进一步提高制备丙烯的转化率。

Description

一种离子液体催化丙烯水合的强化反应系统及工艺 技术领域
本发明涉及异丙醇制备技术领域，尤其涉及一种离子液体催化丙烯水合的强化反应系统及工艺。
背景技术
以丙烯为原料可以通过水合反应制备生产异丙醇，丙烯常温下为无色、稍带有甜味的气体、易燃，爆炸极限为2％～11％，不溶于水，可溶于乙醇、乙醚等有机溶剂，毒性低。
2000年以来我国异丙醇的年产能约为16万吨，产量可达12万吨，然而我国异丙醇的年需求量可达23万吨，证明异丙醇市场缺口大概有10～15万吨每年，因此，每年我国需要进口大量异丙醇，近年来，整个亚太地区异丙醇生产量增加显著，异丙醇市场竞争激烈，对于异丙醇生产工艺的研究与改进意义重大。
目前，异丙醇工业化生产方法主要分为丙烯间接水合法和丙烯直接水合法，丙烯间接水合法对丙烯气体纯度要求较低，并且丙烯转化率较高，但该方法工艺过程复杂，反应过程需要大量的水蒸气，硫酸对设备有腐蚀作用，环境污染较为严重，因此已被直接水合法逐渐取代。
丙烯气相直接水合法又分为气相直接水合法制备异丙醇和液相直接水合法制备异丙醇，液相直接水合法是一种选用活性、稳定性、选择性能都良好的钨系杂多酸催化剂催化丙烯直接水合反应的方法。反应原料丙烯经过加热装置预热通入反应器，催化剂溶解于工艺反应水中进入反应器，此方法的反应温度为240～280℃，压力为20Mpa，原料丙烯与水、催化剂进行接触反应，生成异丙醇存在于溶液中，催化剂钨系多阴离子的水溶液具有较高的活性与寿命，可以获得较高的丙烯单程转化率。但该方法在使用过程中存在明显缺点与不足：
在丙烯气体和离子液体催化剂接触过程中，气液两项混合，产生较大较多气泡，由于气泡较多较大，致使气液两项无法充分混合，导致反应需要在较高预设条件下才能进行，即需要较高的反应温度和反应压力。
发明内容
为此，本发明提供一种离子液体催化丙烯水合的强化反应系统及工艺，用以降低现有技术中采用液相直接水合法制备异丙醇的预设条件。
一方面，本发明提供一种离子液体催化丙烯水合的强化反应系统，包括：
反应器，用以为去离子水、催化剂和丙烯提供反应场所制备异丙醇；
微界面发生器，其将气体的压力能和/或液体的动能转变为气泡表面能并传递给气体反应物，将气体反应物丙烯破碎形成直径≥1μm、且＜1mm的微米级气泡，以提高气体反应物与液体反应物之间的传质面积、减小液膜厚度、降低传质阻力；
预热装置，其与所述微界面发生器相连通，用以对进入所述微界面发生器的丙烯进行预热；
气液分离器，其与所述反应器相连通，用以对产物进行一次分离处理；
共沸塔，其与所述气液分离器相连通，用以对产物进行二次分离处理。
进一步的，所述微界面发生器为气动式微界面发生器，所述微界面发生器位于所述反应器内部，所述微界面发生器用以将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内与所述反应器内的离子液体催化剂混合形成气液乳化物。
进一步的，所述预热装置内设置有循环预热管，通过向所述循环预热管内通入热流体使所述预热装置对丙烯具有预热作用，所述预热装置的一侧设置有第一泵体和换热器，通过所述第一泵体使热流体在所述循环预热管内循环，通过所述换热器保持热流体温度。
进一步的，所述微界面发生器上连通设置有丙烯传输管，所述丙烯传输管与所述预热装置之间设置有第二泵体，通过所述第二泵体将预热后的丙烯沿所述丙烯传输管传输至所述微界面发生器。
进一步的，所述反应器上连通设置有去离子水进入管和催化剂进入管，所述去离子水进入管和所述催化剂进入管用以供去离子水和催化剂进入所述反应器内。
进一步的，所述反应器和所述气液分离器之间通过物料传输管相连通，所述物料传输管上安装有第三泵体，通过所述第三泵体将所述反应器内生成的产物沿 所述物料传输管传输至所述气液分离器内。
进一步的，所述气液分离器和所述预热装置之间设置有第四泵体，通过所述第四泵体将所述气液分离器内气相丙烯传输回所述预热装置，所述气液分离器和所述共沸塔之间设置有第五泵体，通过所述第五泵体将所述气液分离器内液相产物传输至所述共沸塔。
进一步的，所述共沸塔与所述反应器之间设置有第六泵体，通过所述第六泵体将所述共沸塔底部含有催化剂的液体传输回所述反应器内重复使用。
另一方面，本发明提供一种离子液体催化丙烯水合的强化反应工艺，包括：
步骤1：通过所述去离子水进入管和所述催化剂进入管向反应器内加入去离子水和催化剂，并将两者混合均匀成离子液体催化剂；
步骤2：通过所述第一泵体工作将热流体通入所述循环预热管内循环，通过所述换热器工作保持热流体温度，向预热装置内通入丙烯，热流体使所述预热装置对丙烯具有预热作用，通过所述第二泵体工作将预热后的丙烯沿所述丙烯传输管传输至所述微界面发生器；
步骤3：所述微界面发生器工作将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内与所述反应器内的离子液体催化剂混合形成气液乳化物，丙烯发生水合反应；
步骤4：通过所述第三泵体工作将所述反应器内生成的产物沿所述物料传输管传输至所述气液分离器内，产物在所述气液分离器内经冷凝分离为未反应的气相丙烯和液相产物，通过所述第四泵体工作将所述气液分离器内气相丙烯传输回所述预热装置，再次作为原料参与反应，通过所述第五泵体工作将所述气液分离器内液相产物传输至所述共沸塔；
步骤5：液相产物在所述共沸塔内进行分离提浓，塔顶得到异丙醇溶液，塔底得到含有催化剂的溶液，通过所述第六泵体工作将所述共沸塔底部含有催化剂的液体传输回所述反应器内重复使用。
进一步的，所述反应器内的温度为200～220℃，压力为14～16Mpa。
与现有技术相比，本发明的有益效果在于，本发明通过破碎丙烯气体使其形成微米尺度的微米级气泡，微米级气泡具备常规气泡所不具备的理化性质，由球体体积及表面积的计算公式可知，在总体积不变的情况下，气泡的总表面积与单 个气泡直径成反比，由此可知微米级气泡的总表面积巨大，使微米级气泡与离子液体催化剂混合形成气液乳化物，以增大气液两相的接触面积，并达到在较低预设操作条件范围内强化传质的效果，同时也在一定程度上进一步提高制备丙烯的转化率；
进一步的，反应器，用以为去离子水、催化剂和丙烯提供反应场所制备异丙醇；
微界面发生器，其将气体的压力能和/或液体的动能转变为气泡表面能并传递给气体反应物，将气体反应物丙烯破碎形成直径≥1μm、且＜1mm的微米级气泡，以提高气体反应物与液体反应物之间的传质面积、减小液膜厚度、降低传质阻力；
预热装置，其与所述微界面发生器相连通，用以对进入所述微界面发生器的丙烯进行预热；
气液分离器，其与所述反应器相连通，用以对产物进行一次分离处理；
共沸塔，其与所述气液分离器相连通，用以对产物进行二次分离处理。
进一步的，所述微界面发生器为气动式微界面发生器，所述微界面发生器位于所述反应器内部，所述微界面发生器用以将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内与所述反应器内的离子液体催化剂混合形成气液乳化物。
进一步的，所述预热装置内设置有循环预热管，通过向所述循环预热管内通入热流体使所述预热装置对丙烯具有预热作用，所述预热装置的一侧设置有第一泵体和换热器，通过所述第一泵体使热流体在所述循环预热管内循环，通过所述换热器保持热流体温度。
进一步的，所述微界面发生器上连通设置有丙烯传输管，所述丙烯传输管与所述预热装置之间设置有第二泵体，通过所述第二泵体将预热后的丙烯沿所述丙烯传输管传输至所述微界面发生器。通过所述第一泵体工作将热流体通入所述循环预热管内循环，通过所述换热器工作保持热流体温度，向预热装置内通入丙烯，热流体使所述预热装置对丙烯具有预热作用，通过所述第二泵体工作将预热后的丙烯沿所述丙烯传输管传输至所述微界面发生器；
进一步的，所述反应器上连通设置有去离子水进入管和催化剂进入管，所述 去离子水进入管和所述催化剂进入管用以供去离子水和催化剂进入所述反应器内。通过所述去离子水进入管和所述催化剂进入管向反应器内加入去离子水和催化剂，并将两者混合均匀成离子液体催化剂；
进一步的，所述反应器和所述气液分离器之间通过物料传输管相连通，所述物料传输管上安装有第三泵体，通过所述第三泵体将所述反应器内生成的产物沿所述物料传输管传输至所述气液分离器内；
进一步的，所述气液分离器和所述预热装置之间设置有第四泵体，通过所述第四泵体将所述气液分离器内气相丙烯传输回所述预热装置，所述气液分离器和所述共沸塔之间设置有第五泵体，通过所述第五泵体将所述气液分离器内液相产物传输至所述共沸塔；通过所述第三泵体工作将所述反应器内生成的产物沿所述物料传输管传输至所述气液分离器内，产物在所述气液分离器内经冷凝分离为未反应的气相丙烯和液相产物，通过所述第四泵体工作将所述气液分离器内气相丙烯传输回所述预热装置，再次作为原料参与反应，通过所述第五泵体工作将所述气液分离器内液相产物传输至所述共沸塔；
进一步的，所述共沸塔与所述反应器之间设置有第六泵体，通过所述第六泵体将所述共沸塔底部含有催化剂的液体传输回所述反应器内重复使用。液相产物在所述共沸塔内进行分离提浓，塔顶得到异丙醇溶液，塔底得到含有催化剂的溶液，通过所述第六泵体工作将所述共沸塔底部含有催化剂的液体传输回所述反应器内重复使用。
附图说明
图1为本发明所述一种离子液体催化丙烯水合的强化反应系统的结构示意图。
1-反应器、2-微界面发生器、3-预热装置、4-气液分离器、5-共沸塔、6-循环预热管、7-第一泵体、8-换热器、9-丙烯传输管、10-第二泵体、11-去离子水进入管、12-催化剂进入管、13-物料传输管、14-第三泵体、15-第五泵体、16-第六泵体。
具体实施方式
下面参照附图来描述本发明的优选实施方式。本领域技术人员应当理解的是，这些实施方式仅仅用于解释本发明的技术原理，并非在限制本发明的保护范围。
需要说明的是，在本发明的描述中，术语“上”、“下”、“左”、“右”、“内”、“外”等指示的方向或位置关系的术语是基于附图所示的方向或位置关系，这仅仅是为了便于描述，而不是指示或暗示所述装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本发明的限制。
此外，还需要说明的是，在本发明的描述中，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或一体地连接；可以是机械连接，也可以是电连接；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通。对于本领域技术人员而言，可根据具体情况理解上述术语在本发明中的具体含义。
请参阅图1所示，其为本发明提供一种离子液体催化丙烯水合的强化反应系统，包括：
反应器1，用以为去离子水、催化剂和丙烯提供反应场所制备异丙醇；
微界面发生器2，其将气体的压力能和/或液体的动能转变为气泡表面能并传递给气体反应物，将气体反应物丙烯破碎形成直径≥1μm、且＜1mm的微米级气泡，以提高气体反应物与液体反应物之间的传质面积、减小液膜厚度、降低传质阻力，并在破碎后将液体反应物与气体反应物的微米级气泡混合形成气液乳化物，以在较低预设操作条件范围内强化液体反应物与气体反应物之间的传质效率和反应效率；
预热装置3，其与所述微界面发生器相连通，用以对进入所述微界面发生器的丙烯进行预热；
气液分离器4，其与所述反应器相连通，用以对产物进行一次分离处理；
共沸塔5，其与所述气液分离器相连通，用以对产物进行二次分离处理。
请继续参阅图1，所述微界面发生器为气动式微界面发生器，所述微界面发生器位于所述反应器内部，所述微界面发生器用以将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内与所述反应器内的离子液体催化剂混合形成气液乳化物。
请继续参阅图1，所述预热装置内设置有循环预热管6，通过向所述循环预 热管内通入热流体使所述预热装置对丙烯具有预热作用，所述预热装置的一侧设置有第一泵体7和换热器8，通过所述第一泵体使热流体在所述循环预热管内循环，通过所述换热器保持热流体温度。
请继续参阅图1，所述微界面发生器上连通设置有丙烯传输管9，所述丙烯传输管与所述预热装置之间设置有第二泵体10，通过所述第二泵体将预热后的丙烯沿所述丙烯传输管传输至所述微界面发生器。
请继续参阅图1，所述反应器上连通设置有去离子水进入管11和催化剂进入管12，所述去离子水进入管和所述催化剂进入管用以供去离子水和催化剂进入所述反应器内。
请继续参阅图1，所述反应器和所述气液分离器之间通过物料传输管13相连通，所述物料传输管上安装有第三泵体14，通过所述第三泵体将所述反应器内生成的产物沿所述物料传输管传输至所述气液分离器内。
请继续参阅图1，所述气液分离器和所述预热装置之间设置有第四泵体，通过所述第四泵体将所述气液分离器内气相丙烯传输回所述预热装置，所述气液分离器和所述共沸塔5之间设置有第五泵体15，通过所述第五泵体将所述气液分离器内液相产物传输至所述共沸塔。
请继续参阅图1，所述共沸塔5与所述反应器之间设置有第六泵体16，通过所述第六泵体将所述共沸塔底部含有催化剂的液体传输回所述反应器内重复使用。
请继续参阅图1，本发明提供一种离子液体催化丙烯水合的强化反应工艺，包括：
步骤1：通过所述去离子水进入管和所述催化剂进入管向反应器内加入去离子水和催化剂，并将两者混合均匀成离子液体催化剂；
步骤2：通过所述第一泵体工作将热流体通入所述循环预热管内循环，通过所述换热器工作保持热流体温度，向预热装置内通入丙烯，热流体使所述预热装置对丙烯具有预热作用，通过所述第二泵体工作将预热后的丙烯沿所述丙烯传输管传输至所述微界面发生器；
步骤3：所述微界面发生器工作将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内与所述反应器内的离子液体催化 剂混合形成气液乳化物，丙烯发生水合反应；
步骤4：通过所述第三泵体工作将所述反应器内生成的产物沿所述物料传输管传输至所述气液分离器内，产物在所述气液分离器内经冷凝分离为未反应的气相丙烯和液相产物，通过所述第四泵体工作将所述气液分离器内气相丙烯传输回所述预热装置，再次作为原料参与反应，通过所述第五泵体工作将所述气液分离器内液相产物传输至所述共沸塔；
步骤5：液相产物在所述共沸塔内进行分离提浓，塔顶得到异丙醇溶液，塔底得到含有催化剂的溶液，通过所述第六泵体工作将所述共沸塔5底部含有催化剂的液体传输回所述反应器内重复使用。
所述反应器内的温度为200～220℃，压力为14～16Mpa。
实施例1
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为200℃，所述反应器内压强为14Mpa；
所述微界面发生器内的气液比为900：1；
经检测，使用所述系统及工艺后，丙烯单程转化率为81％。
实施例2
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为205℃，所述反应器内压强为14Mpa；
所述微界面发生器内的气液比为900：1；
经检测，使用所述系统及工艺后，丙烯单程转化率为80％。
实施例3
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为210℃，所述反应器内压强为15Mpa；
所述微界面发生器内的气液比为900：1；
经检测，使用所述系统及工艺后，丙烯单程转化率为80％。
实施例4
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为215℃，所述反应器内压强为15Mpa；
所述微界面发生器内的气液比为900：1；
经检测，使用所述系统及工艺后，丙烯单程转化率为82％。
实施例5
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为220℃，所述反应器内压强为16Mpa；
所述微界面发生器内的气液比为900：1；
经检测，使用所述系统及工艺后，丙烯单程转化率为81％。
对比例
使用现有技术丙烯直接水合法进行异丙醇制备，其中，反应器内温度为240℃，压力为20Mpa。
经检测，丙烯单程转化率为67％。
至此，已经结合附图所示的优选实施方式描述了本发明的技术方案，但是，本领域技术人员容易理解的是，本发明的保护范围显然不局限于这些具体实施方式。在不偏离本发明的原理的前提下，本领域技术人员可以对相关技术特征做出等同的更改或替换，这些更改或替换之后的技术方案都将落入本发明的保护范围之内。
以上所述仅为本发明的优选实施例，并不用于限制本发明；对于本领域的技术人员来说，本发明可以有各种更改和变化。凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。

Claims (10)

  1. 一种离子液体催化丙烯水合的强化反应系统，其特征在于，包括：
    反应器，用以为去离子水、催化剂和丙烯提供反应场所制备异丙醇；
    微界面发生器，其将气体的压力能和/或液体的动能转变为气泡表面能并传递给气体反应物，将气体反应物丙烯破碎形成直径≥1μm、且＜1mm的微米级气泡，以提高气体反应物与液体反应物之间的传质面积、减小液膜厚度、降低传质阻力；
    预热装置，其与所述微界面发生器相连通，用以对进入所述微界面发生器的丙烯进行预热；
    气液分离器，其与所述反应器相连通，用以对产物进行一次分离处理；
    共沸塔，其与所述气液分离器相连通，用以对产物进行二次分离处理。
  2. 根据权利要求1所述的一种离子液体催化丙烯水合的强化反应系统，其特征在于，所述微界面发生器为气动式微界面发生器，所述微界面发生器位于所述反应器内部，所述微界面发生器用以将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内与所述反应器内的离子液体催化剂混合形成气液乳化物。
  3. 根据权利要求2所述的一种离子液体催化丙烯水合的强化反应系统，其特征在于，所述预热装置内设置有循环预热管，通过向所述循环预热管内通入热流体使所述预热装置对丙烯具有预热作用，所述预热装置的一侧设置有第一泵体和换热器，通过所述第一泵体使热流体在所述循环预热管内循环，通过所述换热器保持热流体温度。
  4. 根据权利要求2所述的一种离子液体催化丙烯水合的强化反应系统，其特征在于，所述微界面发生器上连通设置有丙烯传输管，所述丙烯传输管与所述预热装置之间设置有第二泵体，通过所述第二泵体将预热后的丙烯沿所述丙烯传输管传输至所述微界面发生器。
  5. 根据权利要求2所述的一种离子液体催化丙烯水合的强化反应系统，其特征在于，所述反应器上连通设置有去离子水进入管和催化剂进入管，所述去离子水进入管和所述催化剂进入管用以供去离子水和催化剂进入所述反应器内。
  6. 根据权利要求2所述的一种离子液体催化丙烯水合的强化反应系统，其特征在于，所述反应器和所述气液分离器之间通过物料传输管相连通，所述物料 传输管上安装有第三泵体，通过所述第三泵体将所述反应器内生成的产物沿所述物料传输管传输至所述气液分离器内。
  7. 根据权利要求2所述的一种离子液体催化丙烯水合的强化反应系统，其特征在于，所述气液分离器和所述预热装置之间设置有第四泵体，通过所述第四泵体将所述气液分离器内气相丙烯传输回所述预热装置，所述气液分离器和所述共沸塔之间设置有第五泵体，通过所述第五泵体将所述气液分离器内液相产物传输至所述共沸塔。
  8. 根据权利要求2所述的一种离子液体催化丙烯水合的强化反应系统，其特征在于，所述共沸塔与所述反应器之间设置有第六泵体，通过所述第六泵体将所述共沸塔底部含有催化剂的液体传输回所述反应器内重复使用。
  9. 一种离子液体催化丙烯水合的强化反应工艺，其特征在于，包括：
    步骤1：通过所述去离子水进入管和所述催化剂进入管向反应器内加入去离子水和催化剂，并将两者混合均匀成离子液体催化剂；
    步骤2：通过所述第一泵体工作将热流体通入所述循环预热管内循环，通过所述换热器工作保持热流体温度，向预热装置内通入丙烯，热流体使所述预热装置对丙烯具有预热作用，通过所述第二泵体工作将预热后的丙烯沿所述丙烯传输管传输至所述微界面发生器；
    步骤3：所述微界面发生器工作将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内与所述反应器内的离子液体催化剂混合形成气液乳化物，丙烯发生水合反应；
    步骤4：通过所述第三泵体工作将所述反应器内生成的产物沿所述物料传输管传输至所述气液分离器内，产物在所述气液分离器内经冷凝分离为未反应的气相丙烯和液相产物，通过所述第四泵体工作将所述气液分离器内气相丙烯传输回所述预热装置，再次作为原料参与反应，通过所述第五泵体工作将所述气液分离器内液相产物传输至所述共沸塔；
    步骤5：液相产物在所述共沸塔内进行分离提浓，塔顶得到异丙醇溶液，塔底得到含有催化剂的溶液，通过所述第六泵体工作将所述共沸塔底部含有催化剂的液体传输回所述反应器内重复使用。
  10. 根据权利要求9所述的一种离子液体催化丙烯水合的强化反应工艺，其 特征在于，所述反应器内的温度为200～220℃，压力为14～16Mpa。
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