CN217549767U - System for be used for continuous production allyl alcohol - Google Patents
System for be used for continuous production allyl alcohol Download PDFInfo
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Abstract
The utility model provides a system for continuous production allyl alcohol, the system includes reactor, gas-liquid separation device, hydrolysis unit, catalyst activation device and rectifier unit, the reactor is equipped with liquid phase feed inlet and gaseous phase feed inlet, the discharge gate of reactor and gas-liquid separation device's feed inlet intercommunication, gas-liquid separation device's liquid phase discharge gate and hydrolysis unit's feed inlet intercommunication, hydrolysis unit's discharge gate and rectifier unit's feed inlet intercommunication, catalyst activation device's discharge gate and hydrolysis unit activator feed inlet intercommunication, rectifier unit's top is equipped with the allyl alcohol discharge gate. A system for continuous production allyl alcohol hydrolyze allyl acetate and the multistep operation of rectification isolation product carries out the coupling with propylene, improved the reactant utilization ratio, reduced material consumption, realized the high-efficient utilization of material, realized low energy consumption, simple, the quick continuous production of allyl alcohol.
Description
Technical Field
The utility model belongs to the chemical synthesis field especially relates to a system for be used for continuous production allyl alcohol.
Background
1, 4-butanediol (1, 4-BDO for short) is an important organic and fine chemical raw material, and is widely applied to the fields of medicine, chemical industry, textile, papermaking, automobile, daily chemical industry and the like. Tetrahydrofuran (THF), polytetramethylene glycol ether (PTMEG), gamma-butyrolactone (GBL), polybutylene succinate (PBS), polybutylene terephthalate (PBT), polyurethane resins (PU Resin), paints and plasticizers, etc., can be produced from 1,4-BDO, as well as brighteners in the solvent and electroplating industries.
Currently, the production processes of 1,4-BDO mainly include (1) an alkynal process, (2) a butadiene acetoxylation process, (3) a Davy process, and (4) a propylene oxide process. The propylene oxide method is also called allyl alcohol method, and mainly comprises the following process flows: propylene and acetic acid are oxidized to synthesize allyl acetate; allyl acetate is hydrolyzed to prepare allyl alcohol; hydroformylation of allyl alcohol to produce 4-hydroxybutanal; hydrogenating 4-hydroxybutyraldehyde to synthesize 1,4-BDO.
The allyl alcohol process has the following advantages over the other three processes: simple process, high utilization value of byproducts, no pollution to the environment, recyclable catalyst, long service life, high product yield, low steam consumption, easy adjustment of production load and low investment in device construction.
In the allyl alcohol process, the synthesis of allyl acetate from propylene and the hydrolysis of allyl acetate are the key steps in the process. In a reaction system for synthesizing allyl acetate from propylene, raw materials comprise propylene, air (oxygen) and acetic acid, products comprise allyl acetate and water, the hydrolysis reaction of the allyl acetate follows, the raw materials comprise allyl acetate and water, and the products comprise allyl alcohol and acetic acid. Therefore, how to connect these two reactions well is the key to reduce the overall process cost.
In addition, during the process of synthesizing allyl acetate from propylene, some heavy component impurities are generated at the same time. These heavy impurities can deactivate the catalyst used for allyl acetate hydrolysis in subsequent steps, eventually forcing the reactor to be shut down, reducing production efficiency.
Patent CN103351279A discloses a method for producing allyl alcohol by using propylene, oxygen and acetic acid. The method couples multiple operations of propylene esterification, strong acid resin catalytic hydrolysis and rectification separation products, and realizes low energy consumption, simple, rapid and continuous production of the allyl alcohol. However, the method does not consider the recovery problem of propylene and oxygen, and causes material loss; the problem of deactivation of the strong acid resin is not considered, and the method cannot be applied to continuous production of allyl alcohol.
Patent CN102892740A discloses a method for removing heavy components by multi-stage distillation to avoid its entering the hydrolysis column and to deactivate the catalyst in the hydrolysis column. This process not only increases cost and energy consumption, but also due to the low content of heavies in the liquid stream (typically less than 1 wt%), removal by distillation is not only inefficient, but also results in loss of useful materials (e.g., acetic acid, allyl acetate).
Patent CN102781903A discloses a method for catalytic degradation of heavy components by using a solid acid catalyst. The catalytic temperature is 140-190 ℃, and the energy consumption is high; in addition, in order to avoid side reactions and avoid the reaction of allyl acetate and acetic acid to obtain propylene glycol diacetate, the performance of the catalyst needs to be strictly controlled, which is not favorable for industrial production.
Therefore, on the basis of the existing preparation process, the coupling of multi-step operations of propylene oxidation, allyl acetate hydrolysis and rectification separation of products is realized, the influence of heavy component impurities on the allyl acetate hydrolysis step is reduced by using a more economical method, and the method becomes a main research direction for realizing efficient and continuous production of allyl alcohol.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims at proposing a system for continuous production allyl alcohol to realize that propylene oxidation, allyl acetate hydrolysis, rectification separation product multistep operation couple.
In order to achieve the above purpose, the technical scheme of the utility model is realized like this:
a system for continuously producing allyl alcohol comprises a reactor, a gas-liquid separation device, a hydrolysis device, a catalyst activation device and a rectification device,
the reactor is provided with a liquid phase feed inlet and a gas phase feed inlet, acetic acid enters the reactor through the liquid phase feed inlet, propylene and oxygen enter the reactor through the gas phase feed inlet, a discharge port of the reactor is communicated with a feed inlet of the gas-liquid separation device,
the liquid phase discharge hole of the gas-liquid separation device is communicated with the feed inlet of the hydrolysis device,
the discharge hole of the hydrolysis device is communicated with the feed inlet of the rectification device,
the discharge hole of the catalyst activation device is communicated with the feed inlet of the activating agent of the hydrolysis device, and preferably, the bottom of the hydrolysis device is also provided with a second discharge hole for discharging the activating agent
And an allyl alcohol discharge port is formed in the top of the rectifying device.
The reactor further comprises a carbon dioxide removing device, a feed inlet of the carbon dioxide removing device is communicated with a gas-phase discharge outlet of the gas-liquid separating device, a discharge outlet of the carbon dioxide removing device is communicated with a gas-phase feed inlet of the reactor, the type of the carbon dioxide removing device is not limited, and all devices capable of removing carbon dioxide in mixed gas are suitable for the system.
Further, a discharge port at the bottom of the rectifying device is communicated with a liquid phase feed inlet of the reactor.
Further, the hydrolysis device is a fixed bed reactor, the number of the fixed bed reactors is two, and the gas-liquid separation device, the catalyst activation device and the rectification device are respectively communicated with the two fixed bed reactors through a three-way valve.
Another object of the utility model is to provide a method for continuous production allyl alcohol to optimize the production technology of allyl alcohol, ensure that the system lasts steady operation, improve utilization of raw materials rate, improve production efficiency, improve the product yield.
In order to achieve the above purpose, the technical scheme of the utility model is realized as follows:
a process for the continuous production of allyl alcohol employing the system as described above comprising the steps of:
s1: injecting acetic acid, propylene, oxygen and a supported palladium catalyst into a reactor, heating to a certain temperature for oxidation reaction, and obtaining a gas-liquid mixture after complete reaction;
s2: injecting the gas-liquid mixture into a gas-liquid separation device for gas-liquid separation to obtain a mixed liquid and a mixed gas, wherein the mixed liquid contains allyl acetate, acetic acid and the like and is discharged from a liquid-phase discharge port, and the mixed gas contains propylene, oxygen, carbon dioxide and the like and is discharged from a gas-phase discharge port;
s3: injecting the mixed solution into a hydrolysis device filled with a solid catalyst, heating to a certain temperature for ester hydrolysis reaction to obtain a crude product containing allyl alcohol;
s4: injecting the crude product into a rectifying device for distillation, discharging light components from a top outlet, collecting gas discharged from the top of the rectifying device, and condensing to obtain the required allyl alcohol;
s5: and injecting the activating agent in the catalyst activating device into the hydrolysis device.
Further, the supported palladium catalyst is a supported catalyst loaded by palladium, copper, zinc and alkali metal acetate, and the preparation method formula is as follows: dipping a catalyst carrier into a solution containing a palladium source, a copper source and a zinc source, and adding an alkaline solution for alkali treatment; after washing to neutrality, the product is optionally reduced; dipping the reduced product into a solution containing alkali metal acetate, and roasting the dipped product to obtain the supported palladium catalyst.
Furthermore, in the step S1, the molar ratio of acetic acid, propylene and oxygen is 0.1-0.2, 1 -1 。
Further, the reaction temperature in the step S3 is 60-100 ℃; preferably, the solid catalyst in step S3 comprises one of a supported solid acid catalyst, an acidic resin, a cation exchange resin, and a supported ester hydrolysis catalyst.
Further, the activating agent comprises one of hydrochloric acid, sulfuric acid and nitric acid; preferably, the concentration of the activator is 0.1 to 8%.
Further, the single running time of each fixed bed reactor in the hydrolysis device is not more than 120h, when the running time of one fixed bed reactor reaches the single running time, the system is switched to the other fixed bed reactor, and the system realizes that the gas-liquid separation device, the catalyst activation device and the rectification device are communicated with different fixed bed reactors through electromagnetic valves.
Further, the method also comprises the following steps:
s6: injecting the mixed gas into a carbon dioxide removal device to obtain recovered gas, wherein the main components in the recovered gas are propylene and oxygen, and injecting the recovered gas into the reactor through a gas-phase feed inlet, so that the recovered gas can be recycled as a gas-phase raw material;
s7: and (3) injecting the recovery liquid discharged from a discharge port at the bottom of the rectifying device into the reactor through the liquid-phase feed inlet by the infusion pump, wherein the main component in the recovery liquid is heavy component acetic acid, and the recovery liquid can be used as a raw material for recycling after being injected into the reactor.
Compared with the prior art, the system for continuously producing allyl alcohol has the following advantages:
(1) The system for continuously producing allyl alcohol couples the multi-step operations of propylene esterification, allyl acetate hydrolysis and rectification separation products, improves the utilization rate of reactants, reduces the material consumption, realizes the high-efficiency utilization of materials, and realizes the low-energy-consumption, simple, rapid and continuous production of allyl alcohol;
(2) A system for continuous production allyl alcohol through simple easy mode of carrying out the circulation activation utilization to the catalyst in the hydrolysis unit, effectively reduced impurity to the influence of hydrolysis catalyst activity under low energy consumption, low-cost prerequisite, maintained the high activity of hydrolysis catalyst, realized that allyl alcohol is continuous, stable, high-efficient production.
Drawings
The accompanying drawings, which form a part of the present disclosure, are included to provide a further understanding of the present disclosure, and are incorporated in and constitute a part of this specification, illustrate embodiments of the present disclosure and together with the description serve to explain the present disclosure. In the drawings:
fig. 1 is a schematic connection structure diagram of a system for continuously producing allyl alcohol according to an embodiment of the present invention.
Description of reference numerals:
1. a liquid phase feed inlet; 2. a gas phase feed inlet; 3. a reactor; 4. a gas-liquid separation device; 5. a carbon dioxide removal device; 6. a hydrolysis device; 7. a catalyst activation device; 8. a rectification device.
Detailed Description
Unless defined otherwise, technical terms used in the following examples have the same meanings as commonly understood by one of ordinary skill in the art to which this invention belongs. The test reagents used in the following examples, unless otherwise specified, were all conventional biochemical reagents; the experimental methods are conventional methods unless otherwise specified.
The present invention will be described in detail with reference to the following embodiments and accompanying drawings.
The system for continuously producing allyl alcohol in the utility model comprises a reactor 3, a gas-liquid separation device 4, a hydrolysis device 6, a catalyst activation device 7, a carbon dioxide removal device 5 and a rectification device 8,
the reactor 3 is provided with a liquid phase feed inlet 1 and a gas phase feed inlet 2, acetic acid enters the reactor 3 through the liquid phase feed inlet 1, propylene and oxygen enter the reactor 3 through the gas phase feed inlet 2, a discharge port of the reactor 3 is communicated with a feed inlet of a gas-liquid separation device 4,
the liquid phase discharge hole of the gas-liquid separation device 4 is communicated with the feed inlet of the hydrolysis device 6,
the feed inlet of the carbon dioxide removing device 5 is communicated with the gas phase discharge outlet of the gas-liquid separating device 4, the discharge outlet of the carbon dioxide removing device 5 is communicated with the gas phase feed inlet 2 of the reactor 3,
the discharge hole of the hydrolysis device 6 is communicated with the feed hole of the rectifying device 8, the hydrolysis device 6 is a fixed bed reactor, the two fixed bed reactors are connected in parallel, the gas-liquid separation device 4, the catalyst activation device 7 and the rectifying device 8 are respectively communicated with the two fixed bed reactors through a three-way valve, the single operation time of each fixed bed reactor in the hydrolysis device 6 is 120 hours,
the discharge hole of the catalyst activation device 7 is communicated with the activating agent feed inlet of the hydrolysis device 6, and the bottom of the hydrolysis device 6 is also provided with a second discharge hole for discharging the activating agent
The top of the rectifying device 8 is provided with an allyl alcohol discharge hole, and the discharge hole at the bottom of the rectifying device 8 is communicated with the liquid-phase feed inlet 1 of the reactor 3.
The utility model discloses a be used for continuous production allyl alcohol's method, including following step:
s1: injecting acetic acid, propylene, oxygen and a supported palladium catalyst into a reactor 3, heating to a certain temperature for oxidation reaction, and obtaining a gas-liquid mixture after the reaction is completed;
s2: injecting the gas-liquid mixture into a gas-liquid separation device 4 for gas-liquid separation to obtain a mixed liquid and a mixed gas;
s3: injecting the mixed solution into a hydrolysis device 6 filled with a solid catalyst, heating to a certain temperature to perform ester hydrolysis reaction to obtain a crude product containing allyl alcohol;
s4: injecting the crude product into a rectifying device 8 for distillation, discharging light components from a top outlet, collecting gas discharged from the top of the rectifying device 8, and condensing to obtain the required allyl alcohol;
s5: injecting the activating agent in the catalyst activating device 7 into the hydrolyzing device 6;
s6: injecting the mixed gas into a carbon dioxide removal device 5 to obtain a recovered gas, wherein the main components of the recovered gas are propylene and oxygen, and injecting the recovered gas into a reactor 3 through a gas-phase feed inlet 2, so that the recovered gas can be recycled as a gas-phase raw material;
s7: the recovery liquid discharged from the bottom discharge hole of the rectifying device 8 is injected into the reactor 3 through the liquid-phase feed inlet 1 by the infusion pump, and the main component in the recovery liquid is the heavy component acetic acid which can be recycled as the raw material when injected into the reactor 3.
Example one
In this example, the reactor 3 is a fixed bed reactor.
The experimental procedure was as described above, wherein:
(a) And (3) oxidation reaction: propylene and oxygen were mixed in a ratio of 5:1 mol ratio is introduced into a reactor 3, and the mol ratio of propylene to acetic acid is 10:1, the catalyst is a supported palladium catalyst, the reaction temperature is 170 ℃, and the reaction pressure is 0.75MPa.
(c) And (3) hydrolysis reaction: the hydrolysis temperature was 80 ℃ and the activator used in the catalyst activation apparatus 7 contained sulfuric acid at a concentration of 3%.
The reaction substrates and products are qualitatively and quantitatively detected by gas chromatography, the conversion rate of the whole acetic acid is 97.6-98.3%, the yield of the allyl alcohol after 24 hours of continuous reaction is 92.1%, and the yield of the allyl alcohol after 2400 hours of continuous reaction is 91.8%.
Example two
In this example, the reactor 3 is a fixed bed reactor.
The experimental procedure was as described above, wherein:
(a) And (3) oxidation reaction: propylene and oxygen were mixed in a ratio of 5:2, introducing the mixture into a reactor 3, wherein the molar ratio of propylene to acetic acid is 10:1, the catalyst is a supported palladium catalyst, the reaction temperature is 160 ℃, and the reaction pressure is 0.6MPa.
(c) And (3) hydrolysis reaction: the hydrolysis temperature was 70 ℃, and the activator used in the catalyst activation device 7 contained 6% hydrochloric acid.
The reaction substrates and products are qualitatively and quantitatively detected by gas chromatography, the conversion rate of the whole acetic acid is 98.1-98.9%, the yield of the allyl alcohol after 24 hours of continuous reaction is 91.7%, and the yield of the allyl alcohol after 2400 hours of continuous reaction is 91.1%.
EXAMPLE III
In this example, the reactor 3 is a tank reactor.
The experimental procedure was as described above, wherein:
(a) And (3) oxidation reaction: propylene and oxygen were mixed in a ratio of 5:1 mol ratio is introduced into a reactor 3, and the mol ratio of propylene to acetic acid is 10:1, the catalyst is a supported palladium catalyst, the reaction temperature is 170 ℃, and the reaction pressure is 0.75MPa.
(c) And (3) hydrolysis reaction: the hydrolysis temperature was 80 ℃ and the activator used in the catalyst activation apparatus 7 contained nitric acid at a concentration of 5%.
The reaction substrates and products are qualitatively and quantitatively detected by gas chromatography, the conversion rate of the whole acetic acid is 97.3-98.4%, the yield of the allyl alcohol after 24 hours of continuous reaction is 92.5%, and the yield of the allyl alcohol after 2400 hours of continuous reaction is 91.5%.
Example four
In this example, the reactor 3 is a moving bed reactor.
The experimental procedure was as described above, wherein:
(a) And (3) oxidation reaction: propylene, oxygen as 5:1 mol ratio is introduced into a reactor 3, and the mol ratio of propylene to acetic acid is 10:1, the catalyst is a supported palladium catalyst, the reaction temperature is 170 ℃, and the reaction pressure is 0.75MPa.
(c) And (3) hydrolysis reaction: the hydrolysis temperature was 80 ℃ and the activator used in the catalyst activation apparatus 7 contained sulfuric acid at a concentration of 3%.
The reaction substrates and products are qualitatively and quantitatively detected by gas chromatography, the conversion rate of the whole acetic acid is 97.8-98.8%, the yield of the allyl alcohol after 24 hours of continuous reaction is 91.9%, and the yield of the allyl alcohol after 2400 hours of continuous reaction is 91.2%.
Comparative example 1
In this comparative example, the reactor 3 was a fixed bed reactor.
The experimental procedure was as described above, wherein:
(a) And (3) oxidation reaction: propylene and oxygen were mixed in a ratio of 5:1 mol ratio is introduced into a reactor 3, and the mol ratio of propylene to acetic acid is 10:1, the catalyst is a supported palladium catalyst, the reaction temperature is 170 ℃, and the reaction pressure is 0.75MPa.
(c) And (3) hydrolysis reaction: the hydrolysis temperature was 80 ℃, and the activating agent used in the catalyst activation device 7 was deionized water.
The reaction substrates and products are qualitatively and quantitatively detected by gas chromatography, the conversion rate of the whole acetic acid is 97.5-98.4%, the yield of the allyl alcohol after 24 hours of continuous reaction is 91.8%, and the yield of the allyl alcohol after 2400 hours of continuous reaction is 53.4%.
Comparative example No. two
In this comparative example, the reactor 3 was a tank reactor.
The experimental procedure was as described above, wherein:
(a) And (3) oxidation reaction: propylene, oxygen as 5:1 mol ratio is introduced into a reactor 3, and the mol ratio of propylene to acetic acid is 10:1, the catalyst is a supported palladium catalyst, the reaction temperature is 170 ℃, and the reaction pressure is 0.75MPa.
(c) And (3) hydrolysis reaction: the hydrolysis temperature is 80 ℃, the whole hydrolysis process is carried out in the same fixed bed reactor, and the hydrolysis catalyst activation treatment is not carried out.
The reaction substrates and products are qualitatively and quantitatively detected by gas chromatography, the conversion rate of the whole acetic acid is 97.5-98.3%, the yield of the allyl alcohol after 24 hours of continuous reaction is 91.7%, and the yield of the allyl alcohol after 2400 hours of continuous reaction is 22.3%.
The results of comparing the acetic acid conversion in the whole course, the allyl alcohol yield after 24 hours of continuous reaction and after 2400 hours of continuous reaction in the first to fourth comparative examples and the first and second comparative examples are shown in Table 1:
TABLE 1 comparison of allyl alcohol yields for the examples and comparative examples
It can be seen from the first to fourth examples and the first and second comparative examples that the catalyst activation device containing the specific activator is adopted to alternately activate two fixed bed reactors connected in parallel in the hydrolysis device, so that the efficient continuous production of the allyl alcohol is realized, and the production efficiency of the system is not obviously reduced after long-time operation.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. A system for the continuous production of allyl alcohol, characterized by: comprises a reactor, a gas-liquid separation device, a hydrolysis device, a catalyst activation device and a rectification device,
the reactor is provided with a liquid phase feed inlet and a gas phase feed inlet, a discharge hole of the reactor is communicated with a feed inlet of the gas-liquid separation device,
the liquid phase discharge hole of the gas-liquid separation device is communicated with the feed inlet of the hydrolysis device,
the discharge hole of the hydrolysis device is communicated with the feed inlet of the rectification device,
the discharge hole of the catalyst activation device is communicated with the feed inlet of the activating agent of the hydrolysis device,
and an allyl alcohol discharge port is formed in the top of the rectifying device.
2. The system of claim 1, wherein: the reactor is characterized by further comprising a carbon dioxide removing device, wherein a feed inlet of the carbon dioxide removing device is communicated with a gas-phase discharge outlet of the gas-liquid separating device, and a discharge outlet of the carbon dioxide removing device is communicated with a gas-phase feed inlet of the reactor.
3. The system of claim 1, wherein: and a discharge hole at the bottom of the rectifying device is communicated with a liquid phase feed inlet of the reactor.
4. The system of claim 1, wherein: the hydrolysis device is a fixed bed reactor, and the number of the fixed bed reactors is two.
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