CN217248803U - Acetaldehyde apparatus for producing - Google Patents
Acetaldehyde apparatus for producing Download PDFInfo
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- CN217248803U CN217248803U CN202220643990.0U CN202220643990U CN217248803U CN 217248803 U CN217248803 U CN 217248803U CN 202220643990 U CN202220643990 U CN 202220643990U CN 217248803 U CN217248803 U CN 217248803U
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- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical compound CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 title claims abstract description 280
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims abstract description 125
- 239000007791 liquid phase Substances 0.000 claims abstract description 46
- 238000004519 manufacturing process Methods 0.000 claims abstract description 35
- 238000011282 treatment Methods 0.000 claims abstract description 16
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical group C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 22
- 238000005191 phase separation Methods 0.000 claims description 21
- 238000010992 reflux Methods 0.000 claims description 20
- 239000007789 gas Substances 0.000 claims description 17
- 238000002309 gasification Methods 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 10
- 239000012071 phase Substances 0.000 claims description 10
- 239000002912 waste gas Substances 0.000 claims description 10
- 238000004065 wastewater treatment Methods 0.000 claims description 7
- 239000002351 wastewater Substances 0.000 abstract description 10
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 abstract description 9
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 3
- 239000007792 gaseous phase Substances 0.000 abstract description 2
- 239000000126 substance Substances 0.000 description 15
- 239000005977 Ethylene Substances 0.000 description 12
- 238000000034 method Methods 0.000 description 11
- 239000000047 product Substances 0.000 description 11
- 239000012535 impurity Substances 0.000 description 10
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 7
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 6
- 230000006872 improvement Effects 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 description 5
- 239000007795 chemical reaction product Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 229920004933 Terylene® Polymers 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 229910052891 actinolite Inorganic materials 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000003674 animal food additive Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- WXZMFSXDPGVJKK-UHFFFAOYSA-N pentaerythritol Chemical compound OCC(CO)(CO)CO WXZMFSXDPGVJKK-UHFFFAOYSA-N 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000005020 polyethylene terephthalate Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses an acetaldehyde apparatus for producing, it includes glycol gasifier, fixed bed reactor, cooler, gas-liquid phase separating tank, buffer tank, vacuum pump, acetaldehyde rectifying column, condenser and backward flow jar, is equipped with entrance point and exit end on the glycol gasifier, and the exit end passes through pipe connection fixed bed reactor, and fixed bed reactor's exit end passes through the pipeline and is connected with gas-liquid phase separating tank, on the pipeline of cooler setting between fixed bed reactor and gas-liquid phase separating tank, the gaseous phase exit linkage exhaust treatment device of gas-liquid phase separating tank, the entrance point of gas-liquid phase exit linkage buffer tank of gas-liquid phase separating tank, the exit end of buffer tank passes through pipe connection acetaldehyde rectifying column, and the top of the tower export of acetaldehyde rectifying column obtains acetaldehyde, discharges waste water at the bottom of the tower. The utility model discloses an acetaldehyde apparatus for producing, simple structure, the equipment that needs is small in quantity, can reduce equipment cost, simplifies production technology, reduces the energy consumption to improve the production efficiency of acetaldehyde, improve the output of acetaldehyde.
Description
Technical Field
The utility model relates to an acetaldehyde production facility field especially relates to an acetaldehyde apparatus for producing.
Background
Acetaldehyde is an important organic chemical intermediate, and has wide application in the fields of pesticides, medicines, foods, feed additives and the like. In 2016, the world acetaldehyde production capacity is more than 218 ten thousand tons per year, the yield is 89 ten thousand tons per year, and the consumption is 88 ten thousand tons per year; the acetaldehyde production capacity in China is 92 ten thousand tons per year, and accounts for about half of the total production energy in the world. In downstream applications of acetaldehyde, pyridine and its derivatives account for the largest proportion of acetaldehyde consumed, 34% (about 30 million tons/year). In addition, pentaerythritol, acetic acid, and acetate account for 23%, 16%, and 10% of the world's acetaldehyde consumption, respectively.
In the prior art, the acetaldehyde production route mainly comprises an ethylene oxidation method, an ethanol oxidation method and an acetylene hydration method. The acetaldehyde production capacity in China is 92 ten thousand tons/year. In china, the ethanol process accounts for the vast majority of acetaldehyde productivity, 85%, and the ethylene process only accounts for 15% of productivity. The ethylene method adopts ethylene as a raw material, so the profit and loss of the ethylene method are greatly influenced by oil price. Because of high oil price, the raw material ethylene has high price, and the devices adopting the ethylene method for petrochemical actinolite 7.5 million tons/year acetaldehyde and petrochemical Shanghai petrochemical 5 million tons/year acetaldehyde are respectively shut down in 2006 and 2011. Correspondingly, the new production capacity mainly adopts ethanol as a raw material, such as a 2-million ton/year acetaldehyde device of Guangxi gold source biochemical industry Co., Ltd and a 10-million ton/year acetaldehyde device of inner Mongolian Linfeng chemical industry.
In the prior art, a production route for producing acetaldehyde by a method of ethylene glycol dehydration is disclosed, ethylene glycol is also known as glycol and is the simplest dihydric alcohol, ethylene glycol is colorless, odorless and sweet liquid and has low toxicity to animals, and ethylene glycol can be mutually soluble in water and acetone but has low solubility in ethers. Used as solvent, antifreezing agent and raw material for synthesizing terylene. At present, the yield of ethylene glycol is rapidly increased, but the demand of acetaldehyde is extremely large, and the existing production equipment for producing acetaldehyde by dehydrating ethylene glycol has the defects of complex production process, high energy consumption and low production efficiency, so that the existing acetaldehyde production equipment needs to be improved to improve the production efficiency of acetaldehyde.
Disclosure of Invention
An object of the utility model is to prior acetaldehyde production facility in the background art, the process is many, the energy consumption is high, low scheduling problem of production efficiency provides an acetaldehyde apparatus for producing.
In order to achieve the above purpose, the utility model discloses a following technical scheme realizes: an acetaldehyde production device comprises an ethylene glycol gasification furnace, a fixed bed reactor, a cooler, a gas-liquid phase separation tank, a buffer tank, a vacuum pump, an acetaldehyde rectifying tower, a condenser and a reflux tank, wherein the ethylene glycol gasification furnace is provided with an inlet end for inputting liquid ethylene glycol and an outlet end for outputting gaseous ethylene glycol, the outlet end of the ethylene glycol gasification furnace is connected with the fixed bed reactor through a pipeline, the outlet end of the fixed bed reactor is connected with the gas-liquid phase separation tank through a pipeline, the cooler is arranged on the pipeline between the fixed bed reactor and the gas-liquid phase separation tank, a gas phase outlet of the gas-liquid phase separation tank is connected with a waste gas treatment device, a liquid phase outlet of the gas-liquid phase separation tank is connected with the inlet end of the buffer tank, the outlet end of the buffer tank is connected with the acetaldehyde rectifying tower through a pipeline, a tower top outlet of the acetaldehyde rectifying tower is connected with the reflux tank through a pipeline, and the condenser is arranged on a connecting pipeline between the tower top outlet of the acetaldehyde rectifying tower and the reflux tank, the gas phase outlet of the reflux tank is connected with a waste gas treatment device, the liquid phase outlet of the reflux tank is an output port of an acetaldehyde product, and the tower bottom liquid of the acetaldehyde rectifying tower is connected with a waste water treatment station.
As a further improvement of the acetaldehyde production device, a preheater for preheating the liquid ethylene glycol is further arranged on a pipeline between the outlet end of the fixed bed reactor and the cooler. Through setting up the pre-heater, can shift the heat that the reaction product of fixed bed reactor's exit end output carried to liquid ethylene glycol in, preheat ethylene glycol, the temperature rise when making liquid ethylene glycol get into the ethylene glycol gasifier can accelerate the gasification rate of ethylene glycol to reduce the energy consumption, reaction product cooling back simultaneously, reentrant cooler can accelerate the cooling speed of reaction product in the cooler, and reduce the cooling load of cooler.
As a further improvement of the acetaldehyde production device, a feeding preheater for preheating the material fed into the acetaldehyde rectifying tower is arranged on a pipeline between the buffer tank and the acetaldehyde rectifying tower. Through setting up the feeding preheater, can make the material that flows to acetaldehyde rectifying column from the buffer tank before getting into acetaldehyde rectifying column, the temperature risees, makes it get into acetaldehyde rectifying column back, and wherein acetaldehyde can gasify more easily, exports from the top of acetaldehyde rectifying column, improves the productivity of acetaldehyde.
As a further improvement of the acetaldehyde production device, a vacuum pump is arranged on a connecting pipeline between a gas phase outlet of the gas-liquid phase separation tank and the waste gas treatment device. Through setting up the vacuum pump, can follow the gas phase export with the gaseous phase material in the gas-liquid phase separating jar and take out and separate, carry to exhaust treatment device, can make impurity in the reaction product discharge from the gas-liquid phase separating jar more easily such as hydrogen, ethylene, carbon monoxide, formaldehyde, improve the purity of the acetaldehyde that obtains.
As a further improvement of the above acetaldehyde production apparatus, the liquid phase outlet end of the reflux drum is connected with the acetaldehyde rectification column through a reflux pipeline. The obtained acetaldehyde can be further rectified as required by arranging a return pipeline, so that the purity of the obtained acetaldehyde is improved.
As a further improvement of the acetaldehyde production device, a booster pump is arranged on a pipeline between the gas-liquid phase separation tank and the buffer tank, and a booster pump is arranged on a pipeline between the buffer tank and the acetaldehyde rectifying tower. Because the gas-liquid phase separation tank is under the negative pressure of 0.03-0.08MPaA, the acetaldehyde rectifying tower is under the micro-positive pressure of 0.105-0.2 MPaA, the negative pressure liquid phase can be pressurized to the positive pressure liquid phase and then enters the acetaldehyde rectifying tower by arranging the booster pumps between the gas-liquid phase separation tank and the buffer tank and between the buffer tank and the acetaldehyde rectifying tower.
As a further improvement of the acetaldehyde production device, a water pump is arranged on a pipeline between the outlet at the bottom of the acetaldehyde rectifying tower and the wastewater treatment station. The discharge speed of the wastewater at the bottom of the tower can be controlled by arranging the water pump.
The utility model discloses has positive effect: the utility model discloses an acetaldehyde apparatus for producing, simple structure, the equipment that needs is small in quantity, can reduce equipment cost, simplifies production technology, reduces the energy consumption to improve the production efficiency of acetaldehyde, improve the output of acetaldehyde.
Drawings
Fig. 1 is a schematic structural diagram of the acetaldehyde production apparatus of the present invention.
The reference numbers in the figures are as follows: the system comprises an ethylene glycol gasification furnace 1, a fixed bed reactor 2, a cooler 3, a gas-liquid phase separation tank 4, a buffer tank 5, a vacuum pump 6, an acetaldehyde rectifying tower 7, a condenser 8, a reflux tank 9, a preheater 10, a feeding preheater 11, a booster pump 12 and a water pump 13.
Detailed Description
The technical solution of the present invention is described in detail and completely by the following embodiments, and it should be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts all belong to the protection scope of the present invention.
The utility model discloses an acetaldehyde apparatus for producing as shown in fig. 1, it includes ethylene glycol gasifier 1, fixed bed reactor 2, cooler 3, gas-liquid phase separation jar 4, buffer tank 5, vacuum pump 6, acetaldehyde rectifying column 7, condenser 8 and reflux drum 9.
The glycol gasification furnace 1 is for gasification of glycol, and since glycol inputted into the fixed bed reactor 2 should be gaseous glycol, the glycol is heated to a high temperature gasification state by the glycol gasification furnace 1.
The fixed bed reactor 2 is provided with a catalyst required for the dehydration reaction of ethylene glycol, and the catalyst is of various types, for example, a molecular sieve catalyst can be selected. In the fixed bed reactor 2, the ethylene glycol undergoes a dehydration reaction at a high temperature to produce acetaldehyde and water. However, during the reaction, there are also side reactions that generate impurities such as hydrogen, carbon monoxide, formaldehyde and ethylene, which are removed in subsequent treatments to increase the purity of the resulting acetaldehyde.
The cooler 3 is used for cooling the gas product output by the fixed bed reactor 2, acetaldehyde can be liquefied through cooling, and meanwhile, impurities such as hydrogen, carbon monoxide and ethylene can be kept in a gaseous state, so that the impurities can be removed through the subsequent gas-liquid phase separation tank 4.
The gas-liquid phase separation tank 4 is used for separating gaseous substances and liquid substances, so that the gaseous substances are output from a gas phase outlet end above the gas-liquid phase separation tank, the gaseous substances are gaseous impurities generated in the fixed bed reactor 2 and comprise hydrogen, ethylene, carbon monoxide and the like, and the gaseous impurities can be pumped to a waste gas treatment device through a connected vacuum pump 6 for further treatment, so that the purity of the obtained acetaldehyde is improved. The waste gas treatment device can select an incinerator, and the impurity gas can be burnt into clean gas through the treatment of the incinerator and then discharged.
The buffer tank 5 is used for storing liquid transmitted from the gas-liquid phase separation tank 4, the main components of the buffer tank 5 are water and acetaldehyde, the working frequencies of the front fixed bed reactor 2 and the rear acetaldehyde rectifying tower 7 can be coordinated by arranging the buffer tank 5, a certain amount of liquid phase substances are conveyed to the acetaldehyde rectifying tower 7 at regular intervals, the working efficiency of the acetaldehyde rectifying tower 7 is guaranteed, and the obtained liquid phase substances can be temporarily stored.
The acetaldehyde rectifying tower 7 is used for gasifying acetaldehyde in liquid phase substances conveyed into the acetaldehyde rectifying tower 5 by the buffer tank, controlling the temperature and reducing the gasification of water as much as possible so as to improve the purity of the obtained acetaldehyde and completely separate the acetaldehyde from the water, the gasified acetaldehyde is output from an outlet at the top of the acetaldehyde rectifying tower 7, the wastewater is discharged from the bottom of the acetaldehyde rectifying tower 7, and the wastewater is conveyed to a wastewater treatment station for further treatment.
The condenser 8 is used for condensing the gasified acetaldehyde output from the acetaldehyde rectifying tower 7 into a liquid state.
The return tank 9 is used for removing gaseous substances in the condensed material, the gaseous substances are mainly gaseous impurities, after the gaseous impurities are removed, the purity of acetaldehyde can be higher, liquid acetaldehyde is output to an acetaldehyde storage container from a liquid phase outlet of the return tank 9 through a water pump 13, or the obtained acetaldehyde is conveyed to an acetaldehyde rectifying tower through a return pipe according to the purity requirement of the acetaldehyde, and is rectified again to improve the purity of the obtained acetaldehyde.
In a preferred embodiment, a preheater 10 for preheating the liquid ethylene glycol is provided in the line between the outlet end of the fixed bed reactor 2 and the cooler 3. Preheater 10 can adopt tubular heat exchanger, the heat that carries the gaseous product of fixed bed reactor 2 output passes through the heat exchange mode transfer to tubular heat exchanger's heat exchange tube, make liquid ethylene glycol pass through tubular heat exchanger earlier before getting into the ethylene glycol gasifier again, preheat ethylene glycol, in order to improve the rate of gasification of ethylene glycol in the ethylene glycol gasifier, and make the heat that the gaseous product carried obtain make full use of, the energy consumption is reduced, and simultaneously, the temperature when also enabling the gaseous product to reach the cooler reduces by a wide margin, be convenient for cool off fast in the cooler, make gaseous acetaldehyde ability fast liquefaction, reduce the heat dissipation load of cooler simultaneously.
As another preferred embodiment, a feed preheater 11 for preheating the material fed into the acetaldehyde rectification column 7 is provided on the piping between the buffer tank 5 and the acetaldehyde rectification column 7. By arranging the feeding preheater 11, the temperature of the material flowing from the buffer tank 5 to the acetaldehyde rectifying tower 7 is raised before the material enters the acetaldehyde rectifying tower 7, so that the acetaldehyde in the material can be gasified more easily after the material enters the acetaldehyde rectifying tower 7, and the acetaldehyde is output from the top end of the acetaldehyde rectifying tower 7, thereby improving the yield of the acetaldehyde.
As another preferred embodiment, a booster pump 12 is arranged on a pipeline between the gas-liquid phase separation tank 4 and the buffer tank 5, and a booster pump 12 is arranged on a pipeline between the buffer tank 5 and the acetaldehyde rectification tower 7. Because the gas-liquid phase separation tank 4 is under the negative pressure of 0.03-0.08MPaA, the acetaldehyde rectifying tower 7 is under the micro-positive pressure of 0.105-0.2 MPaA, the negative pressure liquid phase can be pressurized to the positive pressure liquid phase and then enters the acetaldehyde rectifying tower 7 by arranging the booster pumps 12 between the gas-liquid phase separation tank 4 and the buffer tank 5 and between the buffer tank 5 and the acetaldehyde rectifying tower 7.
As another preferred embodiment, a water pump 13 is arranged on a pipeline between the outlet of the bottom of the acetaldehyde rectification tower 7 and the wastewater treatment station. The discharge speed of the wastewater at the bottom of the tower can be controlled by arranging the water pump 13.
The utility model discloses a feed arrangement is when using, liquid ethylene glycol passes through the heat of preheater absorption fixed bed reactor's gas product earlier, the temperature rises, then heat gasification through the ethylene glycol gasifier again, ethylene glycol gas is from fixed bed reactor's entrance point input, ethylene glycol is under the high temperature condition in fixed bed reactor, and take place dehydration reaction and generate acetaldehyde and water under the effect of molecular sieve catalyst, under the high temperature environment in fixed bed reactor, the reaction product is gaseous state product, gaseous state product is exported from fixed bed reactor's exit end, when the process preheater, the heat that gaseous state product carried is through heat transfer transmission to liquid ethylene glycol, preheat ethylene glycol, and the temperature of gaseous state product also can be reduced, then gaseous state product passes through the cooler again, the temperature descends, make acetaldehyde liquefaction, and impurity gas wherein such as hydrogen, Ethylene, carbon monoxide, formaldehyde and the like are still in gaseous state and are output through a gas phase outlet of a gas-liquid phase separation tank under the suction action of a vacuum pump, the gaseous state is further processed into pollution-free gas in a waste gas treatment device and then discharged, a liquid phase substance containing liquid acetaldehyde is pressurized under the action of a booster pump and then is conveyed to a buffer tank, when the acetaldehyde needs to be input into an acetaldehyde rectifying tower, the liquid phase substance is pressurized under the action of the booster pump and then is heated by a feed preheater, then the liquid phase substance enters the acetaldehyde rectifying tower, the acetaldehyde is gasified under the temperature condition in the acetaldehyde rectifying tower, the gasified acetaldehyde is output from the top of the acetaldehyde rectifying tower, is cooled and condensed into liquid acetaldehyde in a tower top condenser, then enters a reflux tank, the gaseous substance in the reflux tank is conveyed to a waste gas treatment device from a gas phase output port of the reflux tank again, the liquid acetaldehyde is conveyed to an acetaldehyde collection container through a water pump or enters the acetaldehyde rectifying tower again through a reflux pipeline and then is conveyed to the acetaldehyde collection container again And the purity of acetaldehyde is improved, and a valve 13 on the return pipeline is used for controlling the on-off of the return pipeline. And (4) discharging the wastewater at the bottom of the acetaldehyde rectifying tower, conveying the wastewater into a wastewater treatment device under the action of a water pump, and discharging the wastewater after the wastewater is qualified after the wastewater is treated. The utility model discloses an acetaldehyde apparatus for producing, simple structure, the equipment that needs is small in quantity, and simple structure can reduce equipment cost, simplifies production technology, reduces the energy consumption to improve the production efficiency of acetaldehyde, improve the output of acetaldehyde.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. An acetaldehyde apparatus for producing, its characterized in that: the device comprises an ethylene glycol gasification furnace, a fixed bed reactor, a cooler, a gas-liquid phase-splitting tank, a buffer tank, a vacuum pump, an acetaldehyde rectifying tower, a condenser and a reflux tank, wherein the ethylene glycol gasification furnace is provided with an inlet end for inputting liquid ethylene glycol and an outlet end for outputting gaseous ethylene glycol, the outlet end of the ethylene glycol gasification furnace is connected with the fixed bed reactor through a pipeline, the outlet end of the fixed bed reactor is connected with the gas-liquid phase-splitting tank through a pipeline, the cooler is arranged on the pipeline between the fixed bed reactor and the gas-liquid phase-splitting tank, a gas phase outlet of the gas-liquid phase-splitting tank is connected with a waste gas treatment device, a liquid phase outlet of the gas-liquid phase-splitting tank is connected with the inlet end of the buffer tank, the outlet end of the buffer tank is connected with the acetaldehyde rectifying tower, a tower top outlet of the acetaldehyde rectifying tower is connected with the reflux tank through a pipeline, and the condenser is arranged on a connecting pipeline between the tower top outlet of the acetaldehyde rectifying tower and the reflux tank, the gas phase outlet of the reflux tank is connected with a waste gas treatment device, the liquid phase outlet of the reflux tank is an output port of an acetaldehyde product, and the tower bottom liquid of the acetaldehyde rectifying tower is connected with a waste water treatment station.
2. The acetaldehyde production apparatus according to claim 1, wherein: and a preheater for preheating the liquid ethylene glycol is also arranged on a pipeline between the outlet end of the fixed bed reactor and the cooler.
3. The acetaldehyde production apparatus according to claim 1, wherein: and a feeding preheater for preheating the material input into the acetaldehyde rectifying tower is arranged on a pipeline between the buffer tank and the acetaldehyde rectifying tower.
4. The acetaldehyde production apparatus according to claim 1, wherein: and a vacuum pump is arranged on a connecting pipeline between a gas phase outlet of the gas-liquid phase separation tank and the waste gas treatment device.
5. The acetaldehyde production apparatus according to claim 1, wherein: and the liquid phase outlet end of the reflux tank is connected with the acetaldehyde rectifying tower through a reflux pipeline.
6. The acetaldehyde production apparatus according to claim 1, wherein: and a booster pump is arranged on a pipeline between the gas-liquid phase separation tank and the buffer tank, and a booster pump is arranged on a pipeline between the buffer tank and the acetaldehyde rectifying tower.
7. The acetaldehyde production apparatus according to claim 1, wherein: and a water pump is arranged on a pipeline between the outlet at the bottom of the acetaldehyde rectifying tower and the wastewater treatment station.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220643990.0U CN217248803U (en) | 2022-03-22 | 2022-03-22 | Acetaldehyde apparatus for producing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220643990.0U CN217248803U (en) | 2022-03-22 | 2022-03-22 | Acetaldehyde apparatus for producing |
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| Publication Number | Publication Date |
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| CN217248803U true CN217248803U (en) | 2022-08-23 |
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| CN202220643990.0U Active CN217248803U (en) | 2022-03-22 | 2022-03-22 | Acetaldehyde apparatus for producing |
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| CN (1) | CN217248803U (en) |
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- 2022-03-22 CN CN202220643990.0U patent/CN217248803U/en active Active
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