CN213493589U - Reinforced reaction system for catalyzing propylene hydration by ionic liquid - Google Patents
Reinforced reaction system for catalyzing propylene hydration by ionic liquid Download PDFInfo
- Publication number
- CN213493589U CN213493589U CN202020394394.4U CN202020394394U CN213493589U CN 213493589 U CN213493589 U CN 213493589U CN 202020394394 U CN202020394394 U CN 202020394394U CN 213493589 U CN213493589 U CN 213493589U
- Authority
- CN
- China
- Prior art keywords
- propylene
- gas
- reactor
- liquid
- micro
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 91
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 36
- 238000006703 hydration reaction Methods 0.000 title claims abstract description 23
- 230000036571 hydration Effects 0.000 title claims abstract description 20
- 239000002608 ionic liquid Substances 0.000 title claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 76
- 239000003054 catalyst Substances 0.000 claims abstract description 44
- 230000000694 effects Effects 0.000 claims abstract description 10
- 239000000839 emulsion Substances 0.000 claims abstract description 8
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 239000008367 deionised water Substances 0.000 claims description 21
- 229910021641 deionized water Inorganic materials 0.000 claims description 21
- 239000012530 fluid Substances 0.000 claims description 18
- 239000000376 reactant Substances 0.000 claims description 18
- 239000000463 material Substances 0.000 claims description 15
- 239000007791 liquid phase Substances 0.000 claims description 13
- 239000012071 phase Substances 0.000 claims description 11
- 238000006555 catalytic reaction Methods 0.000 abstract description 4
- 238000002360 preparation method Methods 0.000 abstract description 3
- 239000000203 mixture Substances 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 31
- 239000000243 solution Substances 0.000 description 7
- 239000002994 raw material Substances 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000005540 biological transmission Effects 0.000 description 4
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 2
- 229910052721 tungsten Inorganic materials 0.000 description 2
- 239000010937 tungsten Substances 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000011964 heteropoly acid Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 229920000447 polyanionic polymer Polymers 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to an intensive reaction system of ionic liquid catalysis propylene hydration, include: a reactor, a micro-interface generator, a preheating device and the like. The utility model discloses a broken propylene is gaseous to make its micron order bubble that forms micron yardstick, the micron order bubble possesses the physicochemical property that conventional bubble did not possess, can know by the computational formula of spheroid volume and surface area, under the unchangeable condition of total volume, the total surface area and the single bubble diameter inverse ratio of bubble, the total surface area that can know micron order bubble from this is huge, make micron order bubble and ionic liquid catalyst mix and form the gas-liquid emulsion, with the double-phase area of contact of increase gas-liquid, and reach and strengthen the effect of mass transfer at lower predetermined operating condition within range, also further improve the conversion rate of preparation propylene to a certain extent simultaneously.
Description
Technical Field
The utility model relates to an isopropyl alcohol preparation technical field especially relates to a reaction system is reinforceed to ionic liquid catalysis propylene hydration.
Background
Propylene is used as a raw material to prepare the isopropanol through hydration reaction, the propylene is colorless, slightly sweet gas and flammable at normal temperature, the explosion limit is 2-11%, the propylene is insoluble in water, soluble in organic solvents such as ethanol and ether, and low in toxicity.
The annual capacity of isopropanol in China is about 16 ten thousand tons in 2000 years, the yield can reach 12 ten thousand tons, however, the annual demand of isopropanol in China can reach 23 ten thousand tons, and the gap of the isopropanol market is proved to be about 10-15 ten thousand tons per year, so that a large amount of isopropanol needs to be imported in China every year.
At present, the industrial production method of isopropanol mainly comprises a propylene indirect hydration method and a propylene direct hydration method, wherein the propylene indirect hydration method has low requirement on the purity of propylene gas and high conversion rate of propylene, but the method has complex process, a large amount of water vapor is needed in the reaction process, sulfuric acid has corrosion effect on equipment, and the environmental pollution is serious, so the method is gradually replaced by the direct hydration method.
The gas-phase direct hydration method of propylene is divided into a gas-phase direct hydration method for preparing isopropanol and a liquid-phase direct hydration method for preparing isopropanol, and the liquid-phase direct hydration method is a method for catalyzing direct hydration reaction of propylene by using a tungsten heteropoly acid catalyst with good activity, stability and selectivity. The method comprises the steps of preheating reaction raw material propylene by a heating device, introducing the preheated reaction raw material propylene into a reactor, dissolving a catalyst in process reaction water, and introducing the catalyst into the reactor, wherein the reaction temperature of the method is 240-280 ℃, the pressure is 20Mpa, the raw material propylene, water and the catalyst are subjected to contact reaction, generated isopropanol exists in a solution, and the catalyst tungsten polyanion aqueous solution has high activity and service life, and can obtain high propylene single-pass conversion rate. However, the method has obvious disadvantages and shortcomings in the using process:
in the contact process of the propylene gas and the ionic liquid catalyst, the gas and the liquid are mixed to generate more large bubbles, and the gas and the liquid cannot be fully mixed due to the more and the larger bubbles, so that the reaction can be carried out under higher preset conditions, namely higher reaction temperature and reaction pressure are required.
SUMMERY OF THE UTILITY MODEL
Therefore, the utility model provides an ionic liquid catalysis propylene hydration's intensive reaction system for reduce the condition of predetermineeing that adopts the liquid phase direct hydration method to prepare isopropanol among the prior art.
The utility model provides an intensive reaction system of ionic liquid catalysis propylene hydration, include:
the reactor is used for providing reaction sites for deionized water, a catalyst and propylene to prepare isopropanol;
the micro-interface generator converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to a gas reactant, and the propylene of the gas reactant is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, so that the mass transfer area between the gas reactant and the liquid reactant is increased, the thickness of a liquid film is reduced, and the mass transfer resistance is reduced;
the preheating device is communicated with the micro-interface generator and is used for preheating propylene entering the micro-interface generator;
the gas-liquid separator is communicated with the reactor and is used for carrying out primary separation treatment on the product;
and the azeotropic tower is communicated with the gas-liquid separator and is used for carrying out secondary separation treatment on the product.
Furthermore, 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 for crushing propylene to form micron-scale micron-sized bubbles and outputting the micron-scale bubbles into the reactor after the crushing is finished to be mixed with the ionic liquid catalyst in the reactor to form a gas-liquid emulsion.
Furthermore, a circulating preheating pipe is arranged in the preheating device, the preheating device has a preheating effect on propylene by introducing hot fluid into the circulating preheating pipe, a first pump body and a heat exchanger are arranged on one side of the preheating device, the hot fluid is circulated in the circulating preheating pipe through the first pump body, and the temperature of the hot fluid is kept through the heat exchanger.
Furthermore, a propylene conveying pipe is communicated with the micro-interface generator, a second pump body is arranged between the propylene conveying pipe and the preheating device, and the preheated propylene is conveyed to the micro-interface generator along the propylene conveying pipe through the second pump body.
Furthermore, a deionized water inlet pipe and a catalyst inlet pipe are communicated with the reactor and used for allowing deionized water and a catalyst to enter the reactor.
Furthermore, the reactor and the gas-liquid separator are communicated through a material conveying pipe, a third pump body is installed on the material conveying pipe, and a product generated in the reactor is conveyed into the gas-liquid separator along the material conveying pipe through the third pump body.
Further, a fourth pump body is arranged between the gas-liquid separator and the preheating device, the fourth pump body is used for transmitting the gas-phase propylene in the gas-liquid separator back to the preheating device, a fifth pump body is arranged between the gas-liquid separator and the azeotropic tower, and the fifth pump body is used for transmitting the liquid-phase product in the gas-liquid separator to the azeotropic tower.
Further, a sixth pump body is arranged between the azeotropic tower and the reactor, and the liquid containing the catalyst at the bottom of the azeotropic tower is transmitted back to the reactor through the sixth pump body for reuse.
Compared with the prior art, the beneficial effects of the utility model reside in that, the utility model discloses a broken propylene is gaseous to make it form micron order bubble of yardstick, micron order bubble possesses the physicochemical property that conventional bubble did not possess, can know by the computational formula of spheroid volume and surface area, under the unchangeable circumstances of total volume, the total surface area and the single bubble diameter of bubble are inversely proportional, can know from this that micron order bubble's total surface area is huge, make micron order bubble and ionic liquid catalyst mix and form the gas-liquid emulsion, with the area of contact of increase gas-liquid double-phase, and reach the effect of strengthening the mass transfer in lower preset operating condition scope, also improve the conversion rate of preparation propylene to a certain extent simultaneously;
further, the reactor is used for providing reaction sites for deionized water, a catalyst and propylene to prepare isopropanol;
the micro-interface generator converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to a gas reactant, and the propylene of the gas reactant is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, so that the mass transfer area between the gas reactant and the liquid reactant is increased, the thickness of a liquid film is reduced, and the mass transfer resistance is reduced;
the preheating device is communicated with the micro-interface generator and is used for preheating propylene entering the micro-interface generator;
the gas-liquid separator is communicated with the reactor and is used for carrying out primary separation treatment on the product;
and the azeotropic tower is communicated with the gas-liquid separator and is used for carrying out secondary separation treatment on the product.
Furthermore, 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 for crushing propylene to form micron-scale micron-sized bubbles and outputting the micron-scale bubbles into the reactor after the crushing is finished to be mixed with the ionic liquid catalyst in the reactor to form a gas-liquid emulsion.
Furthermore, a circulating preheating pipe is arranged in the preheating device, the preheating device has a preheating effect on propylene by introducing hot fluid into the circulating preheating pipe, a first pump body and a heat exchanger are arranged on one side of the preheating device, the hot fluid is circulated in the circulating preheating pipe through the first pump body, and the temperature of the hot fluid is kept through the heat exchanger.
Furthermore, a propylene conveying pipe is communicated with the micro-interface generator, a second pump body is arranged between the propylene conveying pipe and the preheating device, and the preheated propylene is conveyed to the micro-interface generator along the propylene conveying pipe through the second pump body. The first pump body works to introduce hot fluid into the circulating preheating pipe for circulation, the heat exchanger works to keep the temperature of the hot fluid, propylene is introduced into the preheating device, the hot fluid enables the preheating device to have a preheating effect on the propylene, and the second pump body works to transmit the preheated propylene to the micro-interface generator along the propylene transmission pipe;
furthermore, a deionized water inlet pipe and a catalyst inlet pipe are communicated with the reactor and used for allowing deionized water and a catalyst to enter the reactor. Adding deionized water and a catalyst into the reactor through the deionized water inlet pipe and the catalyst inlet pipe, and uniformly mixing the deionized water and the catalyst to form an ionic liquid catalyst;
further, the reactor and the gas-liquid separator are communicated through a material conveying pipe, a third pump body is mounted on the material conveying pipe, and a product generated in the reactor is conveyed into the gas-liquid separator along the material conveying pipe through the third pump body;
further, a fourth pump body is arranged between the gas-liquid separator and the preheating device, gas-phase propylene in the gas-liquid separator is conveyed 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 liquid-phase products in the gas-liquid separator are conveyed to the azeotropic tower through the fifth pump body; the third pump body works to transmit a product generated in the reactor into the gas-liquid separator along the material transmission pipe, the product is condensed and separated into unreacted gas-phase propylene and liquid-phase product in the gas-liquid separator, the fourth pump body works to transmit the gas-phase propylene in the gas-liquid separator back to the preheating device to participate in reaction as a raw material again, and the fifth pump body works to transmit the liquid-phase product in the gas-liquid separator to the azeotropic tower;
further, a sixth pump body is arranged between the azeotropic tower and the reactor, and the liquid containing the catalyst at the bottom of the azeotropic tower is transmitted back to the reactor through the sixth pump body for reuse. And (3) separating and concentrating the liquid-phase product in the azeotropic tower, obtaining an isopropanol solution at the tower top, obtaining a solution containing the catalyst at the tower bottom, and transmitting the liquid containing the catalyst at the tower bottom back to the reactor for reuse through the operation of the sixth pump body.
Drawings
Fig. 1 is a schematic structural diagram of an enhanced reaction system for catalyzing propylene hydration by using an ionic liquid according to the present invention.
The system comprises a reactor 1, a micro-interface generator 2, a preheating device 3, a gas-liquid separator 4, an azeotropic tower 5, a circulating preheating pipe 6, a first pump body 7, a heat exchanger 8, a propylene conveying pipe 9, a second pump body 10, a deionized water inlet pipe 11, a catalyst inlet pipe 12, a material conveying pipe 13, a third pump body 14, a fifth pump body 15 and a sixth pump body 16.
Detailed Description
Preferred embodiments of the present invention will be described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and do not limit the scope of the present invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Referring to fig. 1, the present invention provides an enhanced reaction system for catalyzing propylene hydration by using ionic liquid, comprising:
a reactor 1 for providing reaction sites for deionized water, a catalyst and propylene to prepare isopropanol;
the micro-interface generator 2 converts pressure energy of gas and/or kinetic energy of liquid into surface energy of bubbles and transmits the surface energy of the bubbles to a gas reactant, propylene of the gas reactant is crushed to form micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm so as to improve the mass transfer area between the gas reactant and the liquid reactant, reduce the thickness of a liquid film and reduce the mass transfer resistance, and the crushed micron-sized bubbles of the liquid reactant and the gas reactant are mixed to form a gas-liquid emulsion so as to strengthen the mass transfer efficiency and the reaction efficiency between the liquid reactant and the gas reactant within a lower preset operating condition range;
the preheating device 3 is communicated with the micro-interface generator and is used for preheating propylene entering the micro-interface generator;
the gas-liquid separator 4 is communicated with the reactor and is used for carrying out primary separation treatment on the product;
and the azeotropic tower 5 is communicated with the gas-liquid separator and is used for carrying out secondary separation treatment on the product.
Referring to fig. 1, 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 configured to crush propylene to form micron-sized bubbles, and after the crushing is completed, the micron-sized bubbles are output to the reactor and mixed with the ionic liquid catalyst in the reactor to form a gas-liquid emulsion.
With continuing reference to fig. 1, a circulating preheating pipe 6 is disposed in the preheating device, the preheating device preheats propylene by introducing a hot fluid into the circulating preheating pipe, a first pump 7 and a heat exchanger 8 are disposed on one side of the preheating device, the hot fluid is circulated in the circulating preheating pipe by the first pump, and the temperature of the hot fluid is maintained by the heat exchanger.
With reference to fig. 1, a propylene delivery pipe 9 is disposed on the micro-interface generator, a second pump body 10 is disposed between the propylene delivery pipe and the preheating device, and the preheated propylene is delivered to the micro-interface generator along the propylene delivery pipe by the second pump body.
With reference to fig. 1, a deionized water inlet pipe 11 and a catalyst inlet pipe 12 are disposed on the reactor in a communicating manner, and the deionized water inlet pipe and the catalyst inlet pipe are used for allowing deionized water and a catalyst to enter the reactor.
With reference to fig. 1, the reactor and the gas-liquid separator are communicated with each other through a material transport pipe 13, a third pump body 14 is installed on the material transport pipe, and a product generated in the reactor is transported into the gas-liquid separator along the material transport pipe through the third pump body.
Referring to fig. 1, a fourth pump is disposed between the gas-liquid separator and the preheating device, the fourth pump is used to transport the gas-phase propylene in the gas-liquid separator back to the preheating device, and a fifth pump 15 is disposed between the gas-liquid separator and the azeotropic tower, and the fifth pump is used to transport the liquid-phase product in the gas-liquid separator to the azeotropic tower.
With continued reference to fig. 1, a sixth pump 16 is disposed between the azeotropic column and the reactor, and the liquid containing the catalyst at the bottom of the azeotropic column is transported back to the reactor for reuse by the sixth pump.
Referring to fig. 1, the present invention provides an enhanced reaction process of catalyzing propylene hydration by ionic liquid, comprising:
step 1: adding deionized water and a catalyst into the reactor through the deionized water inlet pipe and the catalyst inlet pipe, and uniformly mixing the deionized water and the catalyst to form an ionic liquid catalyst;
step 2: the first pump body works to introduce hot fluid into the circulating preheating pipe for circulation, the heat exchanger works to keep the temperature of the hot fluid, propylene is introduced into the preheating device, the hot fluid enables the preheating device to have a preheating effect on the propylene, and the second pump body works to transmit the preheated propylene to the micro-interface generator along the propylene transmission pipe;
and step 3: the micro-interface generator is used for crushing propylene to form micron-sized bubbles, the micron-sized bubbles are output to the reactor after the crushing is finished and are mixed with the ionic liquid catalyst in the reactor to form gas-liquid emulsion, and the propylene is subjected to hydration reaction;
and 4, step 4: the third pump body works to transmit a product generated in the reactor into the gas-liquid separator along the material transmission pipe, the product is condensed and separated into unreacted gas-phase propylene and liquid-phase product in the gas-liquid separator, the fourth pump body works to transmit the gas-phase propylene in the gas-liquid separator back to the preheating device to participate in reaction as a raw material again, and the fifth pump body works to transmit the liquid-phase product in the gas-liquid separator to the azeotropic tower;
and 5: and (3) separating and concentrating the liquid-phase product in the azeotropic tower, obtaining an isopropanol solution at the tower top, obtaining a solution containing the catalyst at the tower bottom, and transmitting the liquid containing the catalyst at the tower bottom back to the reactor for reuse through the operation of the sixth pump body.
The temperature in the reactor is 200-220 ℃, and the pressure is 14-16 Mpa.
Example 1
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 200 ℃, and the pressure in the reactor is 14 Mpa;
the gas-liquid ratio in the micro-interface generator is 900: 1;
after the system and the process are used, the once-through conversion rate of the propylene is 81 percent.
Example 2
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 205 ℃, and the pressure in the reactor is 14 Mpa;
the gas-liquid ratio in the micro-interface generator is 900: 1;
after the system and the process are used, the once-through conversion rate of the propylene is 80 percent.
Example 3
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 210 ℃, and the pressure in the reactor is 15 Mpa;
the gas-liquid ratio in the micro-interface generator is 900: 1;
after the system and the process are used, the once-through conversion rate of the propylene is 80 percent.
Example 4
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 215 ℃, and the pressure in the reactor is 15 Mpa;
the gas-liquid ratio in the micro-interface generator is 900: 1;
after the system and the process are used, the once-through conversion rate of the propylene is 82 percent.
Example 5
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 220 ℃, and the pressure in the reactor is 16 Mpa;
the gas-liquid ratio in the micro-interface generator is 900: 1;
after the system and the process are used, the once-through conversion rate of the propylene is 81 percent.
Comparative example
The isopropanol is prepared by using a propylene direct hydration method in the prior art, wherein the temperature in a reactor is 240 ℃, and the pressure is 20 Mpa.
The once-through conversion of propylene was found to be 67%.
So far, the technical solution of the present invention has been described with reference to the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Without departing from the principle of the present invention, a person skilled in the art can make equivalent changes or substitutions to the related technical features, and the technical solutions after these changes or substitutions will fall within the protection scope of the present invention.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention; various modifications and changes may occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. An enhanced reaction system for catalyzing propylene hydration by ionic liquid, which is characterized by comprising:
the reactor is used for providing reaction sites for deionized water, a catalyst and propylene to prepare isopropanol;
the micro-interface generator converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to a gas reactant, and the gas reactant propylene is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1 mm;
the preheating device is communicated with the micro-interface generator and is used for preheating propylene entering the micro-interface generator;
a gas-liquid separator in communication with the reactor;
an azeotropic column in communication with the gas-liquid separator.
2. The system of claim 1, wherein 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 configured to crush propylene to form micron-sized bubbles and output the micron-sized bubbles into the reactor after the crushing is completed to mix with the ionic liquid catalyst in the reactor to form a gas-liquid emulsion.
3. The system of claim 2, wherein the preheating device is provided with a circulating preheating pipe, the preheating device has a preheating effect on propylene by introducing hot fluid into the circulating preheating pipe, a first pump body and a heat exchanger are arranged on one side of the preheating device, the first pump body is used for circulating the hot fluid in the circulating preheating pipe, and the heat exchanger is used for maintaining the temperature of the hot fluid.
4. The system of claim 2, wherein a propylene transport tube is connected to the micro-interface generator, a second pump is disposed between the propylene transport tube and the preheating device, and the preheated propylene is transported to the micro-interface generator along the propylene transport tube by the second pump.
5. The system of claim 2, wherein 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 allowing deionized water and a catalyst to enter the reactor.
6. The system of claim 2, wherein the reactor is in communication with the gas-liquid separator through a material transfer pipe, and a third pump is mounted on the material transfer pipe, and a product generated in the reactor is transferred into the gas-liquid separator along the material transfer pipe through the third pump.
7. The system as claimed in claim 2, wherein a fourth pump is disposed between the gas-liquid separator and the preheating device, the fourth pump is used to transfer the gas-phase propylene in the gas-liquid separator back to the preheating device, and a fifth pump is disposed between the gas-liquid separator and the azeotropic tower, and the fifth pump is used to transfer the liquid-phase product in the gas-liquid separator to the azeotropic tower.
8. The system of claim 2, wherein a sixth pump is disposed between the azeotrope tower and the reactor, and the liquid containing the catalyst at the bottom of the azeotrope tower is transported back to the reactor for reuse by the sixth pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020394394.4U CN213493589U (en) | 2020-03-25 | 2020-03-25 | Reinforced reaction system for catalyzing propylene hydration by ionic liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020394394.4U CN213493589U (en) | 2020-03-25 | 2020-03-25 | Reinforced reaction system for catalyzing propylene hydration by ionic liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213493589U true CN213493589U (en) | 2021-06-22 |
Family
ID=76378889
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020394394.4U Active CN213493589U (en) | 2020-03-25 | 2020-03-25 | Reinforced reaction system for catalyzing propylene hydration by ionic liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213493589U (en) |
-
2020
- 2020-03-25 CN CN202020394394.4U patent/CN213493589U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2022041426A1 (en) | Micro-interface preparation system and method for cyclic carbonate | |
| WO2022041425A1 (en) | Reinforced micro-interface preparation system and method for cyclic carbonate | |
| CN110981846A (en) | Method for preparing ethylene carbonate by adopting tubular reactor with static mixer | |
| CN111569791A (en) | Enhanced reaction system and process for catalyzing propylene hydration by ionic liquid | |
| WO2022052223A1 (en) | Intensified microinterface preparation system and method for polyglycolic acid | |
| CN213493589U (en) | Reinforced reaction system for catalyzing propylene hydration by ionic liquid | |
| CN104151144A (en) | Method for preparing phenol/acetone by decomposing cumene hydroperoxide | |
| CN112044390A (en) | Preparation system and method of cyclic carbonate | |
| CN111569784B (en) | Sectional type intensified reaction system and process for preparing isopropanol by propylene hydration | |
| CN112499592A (en) | System and process for preparing hydrogen peroxide based on anthraquinone method | |
| CN211814210U (en) | Micro-interface enhanced reaction system for preparing ethylene glycol based on ethylene hydration method | |
| CN207786544U (en) | A kind of lithium salts process units | |
| CN211123731U (en) | Intelligent control reaction system for preparing ethylene glycol based on ethylene hydration method | |
| CN213506673U (en) | 1, 3-diamino-2-hydroxypropane continuous production system | |
| CN212127531U (en) | Nitric acid industry preparation system based on micro-interface is reinforceed | |
| CN109928943B (en) | Method for synthesizing propylene oxide by using microchannel reactor | |
| CN109999728A (en) | A method of reducing the bed temperature rise of HPPO process catalyst | |
| CN115650825A (en) | Method for synthesizing dihydric alcohol monovinyl ether | |
| CN212370135U (en) | Sectional type propylene hydration prepares intensive reaction system of isopropyl alcohol | |
| CN213506658U (en) | Immersed propylene hydration micro-interface enhanced reaction system | |
| CN111569785B (en) | Immersed propylene hydration micro-interface enhanced reaction system and process | |
| CN211725719U (en) | System for reinforcing chloroethane preparation based on micro-interface | |
| CN100391920C (en) | Method for producing substituted benzyl alcohol by continuous process and its apparatus | |
| CN113583032A (en) | Cracking device and method for boron trifluoride complex | |
| CN112694389A (en) | Synthesis method for synthesizing 2,6 di-tert-butyltoluene through heterogeneous catalysis |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |