CN211814209U - Recovery system of methyl alcohol in ethylene glycol production process - Google Patents
Recovery system of methyl alcohol in ethylene glycol production process Download PDFInfo
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- CN211814209U CN211814209U CN202020185759.2U CN202020185759U CN211814209U CN 211814209 U CN211814209 U CN 211814209U CN 202020185759 U CN202020185759 U CN 202020185759U CN 211814209 U CN211814209 U CN 211814209U
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Abstract
The utility model discloses a recovery system of methyl alcohol in ethylene glycol production process, it includes nitric acid storage tank, methyl alcohol storage tank, nitrogen tetroxide storage tank, esterification reactor, carbonylation reaction system, methyl alcohol recovery tower, first cooler, first backward flow jar, torch device, dehydrogenation tower, waste water treatment station, second cooler and second backward flow jar. The utility model has the advantages that the connection structure is simple and easy to realize; the problem of environmental pollution is avoided, and the health and safety of human bodies are ensured; the recycling of the methanol is realized, the waste of resources is avoided, and the economic benefit of enterprises is improved.
Description
The technical field is as follows:
the utility model relates to a chemical industry field of production ethylene glycol, in particular to recovery system of methyl alcohol in ethylene glycol production process.
Background art:
ethylene glycol is a chemical with wide application, is mainly applied to various production fields such as polyester fibers (PET), antifreeze, ethanolamine, explosives and the like, and is used in large quantities as a solvent, a lubricant and a plasticizer. Currently, ethylene glycol production in industry mainly adopts a route of preparing ethylene glycol by gas phase oxidation of petroleum ethylene and then liquid phase catalytic hydration. However, with the international oil price being high for a long time in recent years, the industrial chain for preparing ethylene glycol by using ethylene as a raw material faces huge pressure in the world at present. Therefore, the process for preparing ethylene glycol from coal has attracted more and more attention due to the low production cost; at present, cheap CO and O are utilized2、H2The raw materials such as nitric acid, methanol and the like are subjected to esterification reaction, carbonylation reaction and hydrogenation reaction to produce glycol with high added value; the mixture of dimethyl oxalate (DMO), dimethyl carbonate (DMC), nitrogen monoxide and unreacted methanol and carbon monoxide obtained by carbonylation also needs DMO refining, i.e. the mixture is firstly subjected to gas-liquid separationThen, the liquid is sent to a methanol rectifying tower, the gas is sent to a DMO absorption tower to be washed by methanol, the washed liquid is sent to the methanol rectifying tower to be rectified, the rectified gas is sent to a methanol recovery tower to be recovered by the methanol, and the recovered methanol is stored in a methanol storage tank; sending the rectified liquid into a DMO rectifying tower for rectification, and sending the rectified DMO liquid serving as a production raw material of ethylene glycol into a hydrogenation reactor for reaction to produce ethylene glycol; the rectified gas is recycled to a DMC storage tank to be sold as a product; the following problems exist by adopting the process: the top parts of the methanol storage tank and the DMC storage tank are both provided with an exhaust pipe, and non-condensable gas can be directly discharged at a high point on site through the exhaust pipes, so that the environmental pollution is serious, and even the human health can be injured; meanwhile, the non-condensable gas contains methanol and DMC products, and the direct discharge can cause waste of resources.
The utility model has the following contents:
an object of the utility model is to provide a connection is simple, avoids the polluted environment, and has realized the recovery system of methyl alcohol in resource recovery's the ethylene glycol production process.
The utility model discloses by following technical scheme implement: a methanol recovery system in the ethylene glycol production process comprises a nitric acid storage tank, a methanol storage tank, a dinitrogen tetroxide storage tank, an esterification reactor, a carbonylation reaction system, a methanol recovery tower, a first cooler, a first reflux tank, a torch device, a dehydrogenation tower, a wastewater treatment station, a second cooler and a second reflux tank; the discharge hole of the nitric acid storage tank, the discharge hole of the methanol storage tank and the discharge hole of the dinitrogen tetroxide storage tank are communicated with the feed inlet of the esterification reactor; the gas outlet of the esterification reactor is communicated with the gas inlet of the carbonylation reactor of the carbonylation reaction system; the liquid outlet of the esterification reactor is communicated with the liquid inlet of the methanol recovery tower; the gas outlet of the methanol recovery tower is communicated with the gas inlet of the first cooler, the discharge hole of the first cooler is communicated with the feed inlet of the first reflux tank, and the gas outlet of the first reflux tank is communicated with the gas inlet of the flare device; the liquid outlet of the first reflux tank is communicated with the feed inlet of the esterification reactor; a liquid outlet of the methanol recovery tower is communicated with a liquid inlet of the dehydrogenation tower, a liquid outlet of the dehydrogenation tower is communicated with a liquid inlet of the wastewater treatment station, a gas outlet of the dehydrogenation tower is communicated with a gas inlet of the second cooler, a discharge port of the second cooler is communicated with a feed inlet of the second reflux tank, and a gas outlet of the second reflux tank is communicated with a gas inlet of the torch device; and the liquid outlet of the second reflux tank is communicated with the liquid inlet of the methanol recovery tower.
Further, the carbonylation reaction system comprises a CO source, the carbonylation reactor, a gas-liquid separator, a DMO absorption tower, a methanol rectifying tower, a DMO rectifying tower and a vaporizer; the CO source is communicated with the air inlet of the carbonylation reactor, and the discharge hole of the carbonylation reactor is communicated with the feed inlet of the gas-liquid separator; the gas outlet of the gas-liquid separator is communicated with the gas inlet of the DMO absorption tower; a liquid outlet of the methanol storage tank is communicated with a liquid inlet of the DMO absorption tower, and a gas outlet of the DMO absorption tower is communicated with a feed inlet of the esterification reactor; the liquid outlet of the DMO absorption tower and the liquid outlet of the gas-liquid separator are both communicated with the liquid inlet of the methanol rectifying tower; the gas outlet of the methanol rectifying tower is communicated with the feed inlet of the esterification reactor, the liquid outlet of the methanol rectifying tower is communicated with the liquid inlet of the DMO rectifying tower, the liquid outlet of the DMO rectifying tower is communicated with the liquid inlet of the vaporizer, and the gas outlet of the vaporizer is communicated with the gas inlet of the hydrogenation system.
Further, it comprises a DMC concentration tower, the third cooler, a first buffer tank, a DMC separation tower, a filter, a DMC storage tank, a fourth cooler, and a methanol product storage tank; the liquid outlet of the first reflux drum is communicated with the liquid inlet of the DMC concentration tower; the liquid outlet of the DMC concentration tower is communicated with the liquid inlet of the DMO absorption tower; the gas outlet of the DMC concentration tower and the gas outlet of the DMO rectifying tower are both communicated with the gas inlet of the third cooler, the discharge hole of the third cooler is communicated with the feed inlet of the first cache tank, and the gas outlet of the first cache tank is communicated with the gas inlet of the DMO absorption tower; the liquid outlet of the first buffer tank is communicated with the liquid inlet of the DMC separation tower, and the liquid outlet of the DMC separation tower is communicated with the liquid inlet of the filter; the liquid outlet of the filter is communicated with the liquid inlet of the DMC storage tank; and the gas outlet of the DMC separation tower is communicated with the gas inlet of the fourth cooler, and the liquid outlet of the fourth cooler is communicated with the liquid inlet of the methanol product storage tank.
The utility model has the advantages that: 1. the utility model has simple connection structure and easy realization; the gas separated from the methanol recovery tower is cooled by the first cooler and recovered into the first reflux tank, and the non-condensable gas in the first reflux tank is burnt by the torch device, so that the problem of environmental pollution is avoided, and the health safety of human bodies is ensured; 2. gas separated from the DMC separation tower is condensed into liquid through a fourth cooler and is recycled into a methanol product storage tank to be sold as a product, so that the recycling of methanol is realized, and the economic benefit of enterprises is improved; 3. part of methanol liquid in the first reflux tank is returned to the esterification reactor as a raw material, and DMC liquid separated by the DMC separation tower is recovered to the DMC storage tank after being filtered by the filter and sold as a product, so that methanol recovery is realized, DMC purification is realized, resource waste is avoided, and economic benefits of enterprises are improved.
Description of the drawings:
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic view of the overall structure of the present invention.
Nitric acid storage tank 1, methanol storage tank 2, dinitrogen tetroxide storage tank 3, esterification reactor 4, carbonylation reaction system 5, CO source 5.1, carbonylation reactor 5.2, gas-liquid separator 5.3, DMO absorption tower 5.4, methanol rectifying tower 5.5, DMO rectifying tower 5.6, vaporizer 5.7, methanol recovery tower 6, first cooler 7, first reflux tank 8, flare apparatus 9, dehydrogenation tower 10, wastewater treatment station 11, second cooler 12, second reflux tank 13, DMC concentrating tower 14, third cooler 15, first buffer tank 16, DMC separation tower 17, filter 18, DMC storage tank 19, fourth cooler 20, methanol product storage tank 21, hydrogenation system 22.
The specific implementation mode is as follows:
as shown in fig. 1, a methanol recovery system in ethylene glycol production process comprises a nitric acid storage tank 1, a methanol storage tank 2, a dinitrogen tetroxide storage tank 3, an esterification reactor 4, a carbonylation reaction system 5, a methanol recovery tower 6, a first cooler 7, a first reflux tank 8, a flare device 9, a dehydrogenation tower 10, a wastewater treatment station 11, a second cooler 12, a second reflux tank 13, a DMC concentration tower 14, a third cooler 15, a first buffer tank 16, a DMC separation tower 17, a filter 18, a DMC storage tank 19, a fourth cooler 20 and a methanol product storage tank 21; the discharge hole of the nitric acid storage tank 1, the discharge hole of the methanol storage tank 2 and the discharge hole of the dinitrogen tetroxide storage tank 3 are all communicated with the feed inlet of the esterification reactor 4; the gas outlet of the esterification reactor 4 is communicated with the gas inlet of a carbonylation reactor 5.2 of a carbonylation reaction system 5; the liquid outlet of the esterification reactor 4 is communicated with the liquid inlet of the methanol recovery tower 6; a gas outlet of the methanol recovery tower 6 is communicated with a gas inlet of a first cooler 7, a discharge hole of the first cooler 7 is communicated with a feed inlet of a first reflux tank 8, and a gas outlet of the first reflux tank 8 is communicated with a gas inlet of a torch device 9; the liquid outlet of the first reflux tank 8 is communicated with the feed inlet of the esterification reactor 4; a liquid outlet of the methanol recovery tower 6 is communicated with a liquid inlet of a dehydrogenation tower 10, a liquid outlet of the dehydrogenation tower 10 is communicated with a liquid inlet of a wastewater treatment station 11, a gas outlet of the dehydrogenation tower 10 is communicated with a gas inlet of a second cooler 12, a discharge hole of the second cooler 12 is communicated with a feed inlet of a second reflux tank 13, and a gas outlet of the second reflux tank 13 is communicated with a gas inlet of a torch device 9; the liquid outlet of the second reflux tank 13 is communicated with the liquid inlet of the methanol recovery tower 6.
The carbonylation reaction system 5 comprises a CO source 5.1, a carbonylation reactor 5.2, a gas-liquid separator 5.3, a DMO absorption tower 5.4, a methanol rectifying tower 5.5, a DMO rectifying tower 5.6 and a vaporizer 5.7; the CO source 5.1 is communicated with an air inlet of the carbonylation reactor 5.2, and a discharge hole of the carbonylation reactor 5.2 is communicated with a feed inlet of a gas-liquid separator 5.3; the gas outlet of the gas-liquid separator 5.3 is communicated with the gas inlet of the DMO absorption tower 5.4; a liquid outlet of the methanol storage tank 2 is communicated with a liquid inlet of a DMO absorption tower 5.4, and a gas outlet of the DMO absorption tower 5.4 is communicated with a feed inlet of the esterification reactor 4; the liquid outlet of the DMO absorption tower 5.4 and the liquid outlet of the gas-liquid separator 5.3 are both communicated with the liquid inlet of the methanol rectifying tower 5.5; the gas outlet of the methanol rectifying tower 5.5 is communicated with the feed inlet of the esterification reactor 4, the liquid outlet of the methanol rectifying tower 5.5 is communicated with the liquid inlet of the DMO rectifying tower 5.6, the liquid outlet of the DMO rectifying tower 5.6 is communicated with the liquid inlet of the vaporizer 5.7, and the gas outlet of the vaporizer 5.7 is communicated with the gas inlet of the hydrogenation system 22.
The liquid outlet of the first reflux tank 8 is communicated with the liquid inlet of the DMC concentration tower 14; the liquid outlet of the DMC concentration tower 14 is communicated with the liquid inlet of the DMO absorption tower 5.4; the gas outlet of the DMC concentration tower 14 and the gas outlet of the DMO rectifying tower 5.6 are both communicated with the gas inlet of a third cooler 15, the discharge hole of the third cooler 15 is communicated with the feed inlet of a first cache tank 16, and the gas outlet of the first cache tank 16 is communicated with the gas inlet of a DMO absorption tower 5.4; the liquid outlet of the first buffer tank 16 is communicated with the liquid inlet of a DMC separation tower 17, and the liquid outlet of the DMC separation tower 17 is communicated with the liquid inlet of a filter 18; the liquid outlet of the filter 18 is communicated with the liquid inlet of the DMC storage tank 19; the gas outlet of the DMC separation tower 17 is communicated with the gas inlet of a fourth cooler 20, and the liquid outlet of the fourth cooler 20 is communicated with the liquid inlet of a methanol product storage tank 21.
The working process is as follows: when the esterification reactor 4 is started, methanol, nitric acid and dinitrogen tetroxide are introduced; carrying out reaction to obtain Methyl Nitrite (MN), and reacting the MN with CO in a carbonylation reactor 5.2 to obtain DMO, DMC and NO, and unreacted MN, methanol, CO and the like; sending the solution reacted in the carbonylation reactor 5.2 to a gas-liquid separator 5.3 for gas-liquid separation, sending the separated gas to a DMO absorption tower 5.4 to be cleaned by methanol, sending the gas which is not dissolved in the methanol solution after cleaning back to the esterification reactor 4 to participate in the reaction, wherein the gas also contains gases such as DMC, NO and the like; wherein NO is recycled as raw material, the introduction of dinitrogen tetroxide is stopped, MN, DMC and DMO dissolved in methanol solution and liquid separated from a gas-liquid separator 5.3 are all sent to a methanol rectifying tower 5.5 for rectification, the rectified gas is sent to an esterification reactor 4 to participate in reaction again, the rectified liquid is sent to a DMO rectifying tower 5.6 for rectification, the rectified DMO liquid is sent to a hydrogenation system 22 to react with hydrogen to produce ethylene glycol after being gasified by a vaporizer 5.7 as raw material for producing ethylene glycol.
The solution at the bottom of the esterification reactor 4 is sent to a methanol recovery tower 6 for gas-liquid separation, the separated gas is sent to a first cooler 7 to be cooled into liquid and sent to a first reflux tank 8 for temporary storage, and the non-condensable gas is sent to a torch device 9 for combustion treatment, so that the problem of environmental pollution is avoided, and the health safety of human bodies is ensured; a part of the liquid in the first reflux tank 8 is sent to the esterification reactor 4 to be used as a raw material for reaction again, so that the recovery of methanol is realized, the waste of resources is avoided, and the economic benefit of enterprises is improved; while the other part is sent to the DMC concentration tower 14 for rectification concentration, the solution is rectified and concentrated, and the rectified liquid is sent to a DMO absorption tower 5.4 for washing gas; the rectified gas and the gas rectified from the DMO rectifying tower 5.6 are sent to a third cooler 15 to be cooled into liquid and sent to a first buffer tank 16 for temporary storage, and the non-condensable gas is sent to a DMO absorption tower 5.4 to be washed by methanol solution again; the liquid in the first buffer tank 16 is sent to a DMC separation tower 17 for separation, the separated liquid is filtered by a filter 18, and high-quality DMC is obtained and stored in a DMC storage tank 19 to be sold as a product, so that DMC purification is realized, resource waste is avoided, and economic benefits of enterprises are improved; after being cooled into liquid by the fourth cooler 20, the rectified gas is recycled to the methanol product storage tank 21 and sold as a product, so that the recycling of methanol is realized, and the economic benefit of enterprises is improved; the utility model discloses connection structure is simple, easily realizes.
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 (3)
1. A recovery system of methanol in the production process of ethylene glycol is characterized by comprising a nitric acid storage tank, a methanol storage tank, a dinitrogen tetroxide storage tank, an esterification reactor, a carbonylation reaction system, a methanol recovery tower, a first cooler, a first reflux tank, a torch device, a dehydrogenation tower, a wastewater treatment station, a second cooler and a second reflux tank; the discharge hole of the nitric acid storage tank, the discharge hole of the methanol storage tank and the discharge hole of the dinitrogen tetroxide storage tank are communicated with the feed inlet of the esterification reactor; the gas outlet of the esterification reactor is communicated with the gas inlet of the carbonylation reactor of the carbonylation reaction system; the liquid outlet of the esterification reactor is communicated with the liquid inlet of the methanol recovery tower; the gas outlet of the methanol recovery tower is communicated with the gas inlet of the first cooler, the discharge hole of the first cooler is communicated with the feed inlet of the first reflux tank, and the gas outlet of the first reflux tank is communicated with the gas inlet of the flare device; the liquid outlet of the first reflux tank is communicated with the feed inlet of the esterification reactor; a liquid outlet of the methanol recovery tower is communicated with a liquid inlet of the dehydrogenation tower, a liquid outlet of the dehydrogenation tower is communicated with a liquid inlet of the wastewater treatment station, a gas outlet of the dehydrogenation tower is communicated with a gas inlet of the second cooler, a discharge port of the second cooler is communicated with a feed inlet of the second reflux tank, and a gas outlet of the second reflux tank is communicated with a gas inlet of the torch device; and the liquid outlet of the second reflux tank is communicated with the liquid inlet of the methanol recovery tower.
2. The recycling system of methanol in the ethylene glycol production process according to claim 1, wherein the carbonylation reaction system comprises a CO source, the carbonylation reactor, a gas-liquid separator, a DMO absorption tower, a methanol rectification tower, a DMO rectification tower and a vaporizer; the CO source is communicated with the air inlet of the carbonylation reactor, and the discharge hole of the carbonylation reactor is communicated with the feed inlet of the gas-liquid separator; the gas outlet of the gas-liquid separator is communicated with the gas inlet of the DMO absorption tower; a liquid outlet of the methanol storage tank is communicated with a liquid inlet of the DMO absorption tower, and a gas outlet of the DMO absorption tower is communicated with a feed inlet of the esterification reactor; the liquid outlet of the DMO absorption tower and the liquid outlet of the gas-liquid separator are both communicated with the liquid inlet of the methanol rectifying tower; the gas outlet of the methanol rectifying tower is communicated with the feed inlet of the esterification reactor, the liquid outlet of the methanol rectifying tower is communicated with the liquid inlet of the DMO rectifying tower, the liquid outlet of the DMO rectifying tower is communicated with the liquid inlet of the vaporizer, and the gas outlet of the vaporizer is communicated with the gas inlet of the hydrogenation system.
3. The system of claim 2, further comprising a DMC concentration tower, a third cooler, a first buffer tank, a DMC separation tower, a filter, a DMC storage tank, a fourth cooler, and a methanol product storage tank; the liquid outlet of the first reflux drum is communicated with the liquid inlet of the DMC concentration tower; the liquid outlet of the DMC concentration tower is communicated with the liquid inlet of the DMO absorption tower; the gas outlet of the DMC concentration tower and the gas outlet of the DMO rectifying tower are both communicated with the gas inlet of the third cooler, the discharge hole of the third cooler is communicated with the feed inlet of the first cache tank, and the gas outlet of the first cache tank is communicated with the gas inlet of the DMO absorption tower; the liquid outlet of the first buffer tank is communicated with the liquid inlet of the DMC separation tower, and the liquid outlet of the DMC separation tower is communicated with the liquid inlet of the filter; the liquid outlet of the filter is communicated with the liquid inlet of the DMC storage tank; and the gas outlet of the DMC separation tower is communicated with the gas inlet of the fourth cooler, and the liquid outlet of the fourth cooler is communicated with the liquid inlet of the methanol product storage tank.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202020185759.2U CN211814209U (en) | 2020-02-18 | 2020-02-18 | Recovery system of methyl alcohol in ethylene glycol production process |
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| CN202020185759.2U CN211814209U (en) | 2020-02-18 | 2020-02-18 | Recovery system of methyl alcohol in ethylene glycol production process |
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| CN211814209U true CN211814209U (en) | 2020-10-30 |
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| CN202020185759.2U Active CN211814209U (en) | 2020-02-18 | 2020-02-18 | Recovery system of methyl alcohol in ethylene glycol production process |
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