CN210595848U - Purge gas and carbon four-residue comprehensive recovery system in butadiene production - Google Patents
Purge gas and carbon four-residue comprehensive recovery system in butadiene production Download PDFInfo
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- CN210595848U CN210595848U CN201921567257.XU CN201921567257U CN210595848U CN 210595848 U CN210595848 U CN 210595848U CN 201921567257 U CN201921567257 U CN 201921567257U CN 210595848 U CN210595848 U CN 210595848U
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Abstract
The utility model discloses a recovery system is synthesized to purge gas and four residual of carbon in butadiene production, including four raw materials buffer tanks of carbon, first rectifying column backward flow jar, second rectifying column backward flow jar, butene raw materials buffer tank, air compressor machine, steam source, dehydrogenation reactor, water-cooling acid washing tower, compressor, oil absorption tower, absorption oil desorption tower, first extraction rectifying column, second extraction rectifying column, crude butadiene water washing tower, butadiene dehydration tower, butadiene rectifying column and recovery rectifying column. According to the scheme, the recovery rectifying tank is arranged, heavy component butene-1, cis-butene and isobutane in the carbon four raffinate and purge gas are returned to the butylene raw material buffer tank of the oxidative dehydrogenation unit to be used as oxidative dehydrogenation raw materials, the light component is discharged to a torch to be combusted, the utilization rate of the carbon four raw material is improved, the energy-saving and emission-reduction effect of the device is obvious, and the economic benefit is obvious.
Description
The technical field is as follows:
the utility model relates to a recovery system especially relates to a recovery system is synthesized to speed gassing and four residual liquids of carbon in butadiene production.
Background art:
butadiene is colorless and slightly garlic-like gas at normal temperature and normal pressure, the normal pressure boiling point is-4.4 ℃, the butadiene is mainly used for producing synthetic rubber, for example, butadiene and styrene can be copolymerized to produce butadiene-styrene rubber, butadiene can be subjected to directional polymerization reaction under the action of a catalyst to produce butadiene rubber, butadiene and acrylonitrile are copolymerized to produce nitrile-butadiene rubber and the like.
The main production method of butadiene is a butylene oxidative dehydrogenation method, the production system comprises an MTBE unit, an oxidative dehydrogenation unit and a butadiene extraction unit, and the MTBE unit comprises a four-carbon raw material buffer tank, a first rectifying tower reflux tank, a second rectifying tower and a second rectifying tower reflux tank; the oxidative dehydrogenation unit comprises a butylene raw material buffer tank, an air compressor, a steam source, a dehydrogenation reactor, a water-cooled acid washing tower, a compressor, an oil absorption tower and an absorption oil desorption tower; the butadiene extraction unit comprises a first extraction rectifying tower, a second extraction rectifying tower, a crude butadiene washing tower, a butadiene dehydration tower and a butadiene rectifying tower;
butadiene is generally prepared by adopting a raw material C4 obtained in the process of preparing olefin (MTO) from methanol at present, wherein the raw material C4 mainly contains raw materials of maleic and fumaric, and also comprises impurities such as butene-1, 3-butadiene and isobutene, an MTBE unit is mainly used for purifying the raw material C4, removing the 1, 3-butadiene and isobutene, refining the butene-1, removing the 1, 3-butadiene and isobutene, and rectifying the carbon D after removing the 1, 3-butadiene and isobutene in a first rectifying tower, a first rectifying tower reflux tank, a second rectifying tower and a second rectifying tower reflux tank to obtain a product butene-1 with higher value through refining; the residual butylene raw material is sent into an oxidative dehydrogenation unit for oxidative dehydrogenation reaction, the generated material not only contains butadiene, but also contains byproducts, and crude butadiene is obtained after compression, oil absorption and desorption; the crude butadiene contains butadiene, maleic, fumaric, butane, ethylene and acetylene, the crude butadiene enters a butadiene extraction unit, is subjected to extraction and rectification by a first extraction and rectification tower and a second extraction and rectification tower (acetonitrile is used as an extractant), so that the crude butadiene with the purity of more than 95% is obtained, then enters a crude butadiene washing tower, is washed by water to remove acetonitrile, then enters a butadiene dehydration tower and a butadiene rectification tower, is dehydrated, and is purified to remove trace maleic and fumaric, so that a butadiene product with the purity of more than 99.5% and carbon four residual liquid are obtained.
The problems in the existing butadiene production system are as follows: 1. the carbon four-residue liquid comprises the following components: 98.33 percent; and (3) trans-butene: 0.47%; 1, 3-butadiene: 1.17 percent, trace polymerization inhibitor, butadiene dimer and other heavy components, which are sold without treatment, on one hand, the product has low selling price due to low purity, and on the other hand, the product is used as a raw material for producing butadiene, so that the utilization rate of the raw material is reduced due to the sale; 2. the reflux tank of the first rectifying tower needs to discharge part of purge gas to enter a flare system because of the need of removing light key components such as isobutane, and the purge gas comprises the following components: 1.28%, propylene: 5.63 percent. Propane: 0.94%, dimethyl ether: 9.03%, isobutane: 14.68%, butene-167.99%, butene: 0.01 percent, causes material loss and influences the yield of the device.
The utility model has the following contents:
an object of the utility model is to provide a recovery system is synthesized to purge gas and four residual liquid of carbon in butadiene production.
The utility model discloses by following technical scheme implement: a comprehensive recovery system for purge gas and carbon four-residue in butadiene production comprises a carbon four-raw-material buffer tank, a first rectifying tower reflux tank, a second rectifying tower reflux tank, a butylene raw-material buffer tank, an air compressor, a steam source, a dehydrogenation reactor, a water-cooled acid washing tower, a compressor, an oil absorption tower, an absorption oil desorption tower, a first extraction rectifying tower, a second extraction rectifying tower, a crude butadiene water washing tower, a butadiene dehydration tower and a butadiene rectifying tower;
a discharge hole of the carbon four-material buffer tank is communicated with a feed inlet of the first rectifying tower through a pipeline, a discharge hole of the top of the first rectifying tower is communicated with a feed inlet of a reflux tank of the first rectifying tower through a pipeline, and a discharge hole of the bottom of the reflux tank of the first rectifying tower is communicated with a reflux hole of the first rectifying tower through a pipeline; the tower bottom discharge hole of the first rectifying tower is communicated with the feed inlet of the second rectifying tower through a pipeline; the top of the tower discharge gate of second rectifying column with the feed inlet of second rectifying column reflux tank passes through the pipeline intercommunication, the tank bottoms discharge gate of second rectifying column reflux tank with the backward flow mouth of second rectifying column passes through the pipeline intercommunication, the tank bottoms discharge gate of second rectifying column reflux tank still with the outer butene-1 jar intercommunication of boundary region. The utilization value of the butene-1 is higher, and the butene-1 can be used as a raw material for producing polybutene; a discharge hole at the bottom of the second rectifying tower is communicated with a feed hole of the butene raw material buffer tank through a pipeline;
the butylene raw material buffer tank, the air compressor and the steam source are communicated with a feed inlet of the dehydrogenation reactor through pipelines, a discharge outlet of the dehydrogenation reactor is communicated with a feed inlet of the water-cooling acid washing tower through a pipeline, a discharge outlet of the water-cooling acid washing tower is communicated with a feed inlet of the compressor through a pipeline, a discharge outlet of the compressor is communicated with a feed inlet of the oil absorption tower through a pipeline, a discharge outlet of the oil absorption tower is communicated with a feed inlet of the absorption oil desorption tower through a pipeline, a discharge outlet of the absorption oil desorption tower is communicated with a feed inlet of the first extraction rectification tower through a pipeline, a discharge outlet of the first extraction rectification tower is communicated with a feed inlet of the second extraction rectification tower through a pipeline, a discharge outlet of the second extraction rectification tower is communicated with a feed inlet of the crude butadiene water washing tower through a pipeline, a discharge hole at the top of the crude butadiene washing tower is communicated with a feed inlet of the butadiene dehydrating tower through a pipeline, a discharge hole at the bottom of the butadiene dehydrating tower is communicated with a feed inlet of the butadiene rectifying tower through a pipeline, and a butadiene product is produced at the top of the butadiene rectifying tower and is sent out of the room;
the device is characterized by further comprising a recovery rectifying tower, wherein a feed inlet of the recovery rectifying tower is communicated with a discharge outlet at the bottom of the butadiene dehydration tower through a pipeline, a discharge outlet at the bottom of the recovery rectifying tower is communicated with a butylene raw material buffer tank through a pipeline, and gas at the top of the recovery rectifying tower is sent to a torch for combustion.
Further, a purge gas outlet of the first rectifying tower reflux tank is communicated with a feed inlet of the recovery rectifying tower.
The utility model has the advantages that:
1. according to the scheme, a recovery rectifying tank is arranged, heavy components of butene-1, cis-butene and isobutane in the carbon four raffinate and purge gas are returned to a butene raw material buffer tank of an oxidative dehydrogenation unit, the butene-1 and the cis-butene are used as oxidative dehydrogenation raw materials to produce butadiene, the isobutane is separated in a first extractive rectifying tower, is discharged from the top of the tower and enters a subsequent unit for continuous recovery; the light components (hydrogen, dimethyl ether, propylene and propane) are discharged to a torch for combustion, so that the utilization rate of the raw material carbon four is improved.
2. The scheme recovers the material loss caused by the emission of the purge gas, improves the product yield to a certain extent, has obvious energy-saving and emission-reducing effects on the device and has obvious economic benefit.
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 system diagram of the present embodiment.
In the figure: the system comprises a carbon four-material buffer tank 1, a first rectifying tower 2, a first rectifying tower reflux tank 3, a second rectifying tower 4, a second rectifying tower reflux tank 5, a butylene material buffer tank 6, an air compressor 7, a steam source 8, a dehydrogenation reactor 9, a water-cooling acid washing tower 10, a compressor 11, an oil absorption tower 12, an absorption oil desorption tower 13, a first extraction rectifying tower 14, a second extraction rectifying tower 15, a crude butadiene water washing tower 16, a butadiene dehydration tower 17, a butadiene rectifying tower 18 and a recovery rectifying tower 19.
The specific implementation mode is as follows:
the technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
A comprehensive recovery system for purge gas and carbon four-residue in butadiene production comprises a carbon four-raw material buffer tank 1, a first rectifying tower 2, a first rectifying tower reflux tank 3, a second rectifying tower 4, a second rectifying tower reflux tank 5, a butylene raw material buffer tank 6, an air compressor 7, a steam source 8, a dehydrogenation reactor 9, a water-cooling acid washing tower 10, a compressor 11, an oil absorption tower 12, an absorption oil desorption tower 13, a first extraction rectifying tower 14, a second extraction rectifying tower 15, a crude butadiene water washing tower 16, a butadiene dehydration tower 17 and a butadiene rectifying tower 18;
a discharge hole of the carbon four-material buffer tank 1 is communicated with a feed inlet of the first rectifying tower 2 through a pipeline, a discharge hole of the top of the first rectifying tower 2 is communicated with a feed inlet of a reflux tank 3 of the first rectifying tower through a pipeline, and a discharge hole of the bottom of the reflux tank 3 of the first rectifying tower is communicated with a reflux hole of the first rectifying tower 2 through a pipeline; a tower bottom discharge hole of the first rectifying tower 2 is communicated with a feed inlet of the second rectifying tower 4 through a pipeline; a discharge port at the top of the second rectifying tower 4 is communicated with a feed port of a second rectifying tower reflux tank 5 through a pipeline, a discharge port at the bottom of the second rectifying tower reflux tank 5 is communicated with a reflux port of the second rectifying tower 4 through a pipeline, and a discharge port at the bottom of the second rectifying tower reflux tank 5 is also communicated with a butene-1 tank outside the battery compartment; a discharge hole at the bottom of the second rectifying tower 4 is communicated with a feed inlet of a butylene raw material buffer tank 6 through a pipeline;
the butylene raw material buffer tank 6, the air compressor 7 and the steam source 8 are all communicated with a feed inlet of a dehydrogenation reactor 9 through pipelines, a discharge outlet of the dehydrogenation reactor 9 is communicated with a feed inlet of a water-cooling acid washing tower 10 through a pipeline, a discharge outlet of the top of the water-cooling acid washing tower 10 is communicated with a feed inlet of a compressor 11 through a pipeline, a discharge outlet of the compressor 11 is communicated with a feed inlet of an oil absorption tower 12 through a pipeline, a discharge outlet of the bottom of the oil absorption tower 12 is communicated with a feed inlet of an absorption oil desorption tower 13 through a pipeline, a discharge outlet of the middle part of the absorption oil desorption tower 13 is communicated with a feed inlet of a first extraction rectification tower 14 through a pipeline, a discharge outlet of the bottom of the first extraction rectification tower 14 is communicated with a feed inlet of a second extraction rectification tower 15 through a pipeline, a discharge outlet of the top of the second extraction rectification tower 15 is communicated with a feed inlet of a crude butadiene water washing tower 16 through, a discharge hole at the bottom of the butadiene dehydrating tower 17 is communicated with a feed inlet of a butadiene rectifying tower 18 through a pipeline, and a butadiene product is produced at the top of the butadiene rectifying tower 18 and is sent out;
the system also comprises a recovery rectifying tower 19, wherein the temperature of the top of the recovery rectifying tower 19 is controlled to be about 50 ℃, and the temperature of the bottom of the recovery rectifying tower is controlled to be about 70 ℃; the feed inlet of the recovery rectifying tower 19 is communicated with the discharge outlet at the bottom of the butadiene dehydrating tower 17 through a pipeline, the discharge outlet at the bottom of the recovery rectifying tower 19 is communicated with the butylene raw material buffer tank 6 through a pipeline, and the gas at the top of the recovery rectifying tower 19 is sent to a torch for combustion.
The purge gas outlet of the first rectifying tower reflux tank 3 is communicated with the feed inlet of the recovery rectifying tower 19.
The working process is as follows:
feeding the ether carbon IV from the washing into an upper tower 2 of a first rectifying tower for rectifying to remove light components (water, isobutane and the like); the gas at the top of the tower enters a first rectifying tower reflux tank 3 after being condensed by a condenser of the first rectifying tower, is pumped out by a reflux pump and is injected into the top of the tower 2 of the first rectifying tower as reflux, and the non-condensable gas in the first rectifying tower reflux tank 3 enters a recovery rectifying tower 19 after being controlled by a regulating valve.
The material in the bottom of the first rectifying tower 2 is carbon four-fraction from which light components such as isobutane are removed, is pumped out by a tower bottom pump, and is sent to a second rectifying tower 4.
The material from the first rectifying tower 2 is separated in the second rectifying tower 4 to remove heavy components (butylene-2, n-butane and the like). The gas at the top of the second rectifying tower 4 enters a second rectifying tower reflux tank 5 after being condensed by a condenser of the second rectifying tower 4, and then is pressurized by a second rectifying tower reflux pump, a part of the gas is injected into the top of the second rectifying tower 4 as reflux to be continuously rectified, and a part of the gas is sent to a tank area outside the battery compartment as a butene-1 product (the purity is more than or equal to 99%).
The tower bottom material of the second rectifying tower 4 is heavy fraction mainly comprising n-butane and cis-trans-butene-2, and is sent to a butene raw material buffer tank 6 to be used as a raw material of an oxidative dehydrogenation unit.
0.5MPa of blending steam from a steam source 8, a butylene raw material from a butylene raw material buffer tank 6 and air from an air compressor 7 are mixed and then enter a dehydrogenation reactor 9 filled with a catalyst bed layer with a spinel structure for oxidative dehydrogenation.
The temperature in the dehydrogenation reactor 9 is controlled to be 350-380 ℃, and the outlet temperature of the dehydrogenation reactor 9 is controlled to be below 580 ℃, generally about 550 ℃. The generated gas enters a water-cooling acid washing tower 10 after a series of heat exchange (a heat exchanger is not shown in the figure), the temperature of the generated gas is controlled below 95 ℃, fresh water with the temperature of about 5 ℃ is added at the tower top, the generated gas is cooled in the water-cooling acid washing tower 10, a large amount of water and a small amount of acid, aldehyde, ketone and the like are removed, the generated gas flows out of the tower top of the water-cooling acid washing tower 10, enters an oil absorption tower 12 after entering a compressor 11 for compression and pressurization, the carbon four components and non-condensable gas are separated through desorption oil, the non-condensable gas is discharged outside, the desorption oil absorbing the carbon four components is discharged from the tower bottom of the oil absorption tower 12, enters an absorption oil desorption tower 13, and the carbon four components, namely;
the crude butadiene is sent to the (12, 24) th tray of the first extractive distillation column 14; the solvent acetonitrile enters the first extractive distillation tower 14 from the 10 th layer of tower plate of the first extractive distillation tower 14 by using a first extractive solvent pump. The acetonitrile solvent added from the top of the first extractive distillation tower 14 flows to the tower kettle from top to bottom through a tower tray, the crude butadiene raw material is fully contacted with the acetonitrile solvent on the tower tray, so that the relative volatility of the butylene and the butadiene is increased, and the acetonitrile solvent containing the butadiene enters the tower kettle of the first extractive distillation tower 14; cis-butene, trans-butene-2, n-butene and a small amount of butane which are difficult to dissolve in the acetonitrile solvent are distilled out from the top of the first extractive distillation tower 14.
The butadiene and acetonitrile solvent at the bottom of the first extractive distillation tower 14 enters the tower kettle of a second extractive distillation tower 15, and the acetonitrile solvent of the second extractive distillation tower 15 enters from a 16 th layer of tower plate of the second extractive distillation tower 15; and the material at the top of the second extraction and rectification tower 15 enters a butadiene water washing tower 16, and acetonitrile and other substances carried in the crude butadiene are washed away by deoxygenated water. Deoxygenated water enters from the upper part of the butadiene water washing tower 16, crude butadiene enters from the bottom of the butadiene water washing tower 16, the crude butadiene is reversely contacted and washed in the tower, and the crude butadiene with acetonitrile and other impurities washed away is sent to the butadiene dehydration tower 17.
Crude butadiene from butadiene water wash column 16 enters from the 19 th tray of butadiene dehydration column 17. The material in the bottom of the butadiene dehydrating tower 17 is sent to a butadiene rectifying tower 18.
In the butadiene rectifying column 18, butadiene from the butadiene dehydrating column 17 enters the tray 42. The overhead vapor phase is sent to the drum area as butadiene product. Heavy components in a tower bottom of a butadiene rectifying tower 18 and non-condensable gas materials at the top of a first rectifying tower reflux tank 3 are converged and enter a recovery rectifying tower 19, four components of tower bottom carbon of the recovery rectifying tower 19 are pressurized by a tower bottom pump and then sent to a butylene raw material buffer tank 6 to be used as a raw material for oxidative dehydrogenation, and non-condensable gas at the tower top of the recovery rectifying tower 19 is sent to a torch system for combustion after pressure control.
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 (2)
1. A comprehensive recovery system for purge gas and carbon four-residue in butadiene production comprises a carbon four-raw-material buffer tank, a first rectifying tower reflux tank, a second rectifying tower reflux tank, a butylene raw-material buffer tank, an air compressor, a steam source, a dehydrogenation reactor, a water-cooled acid washing tower, a compressor, an oil absorption tower, an absorption oil desorption tower, a first extraction rectifying tower, a second extraction rectifying tower, a crude butadiene water washing tower, a butadiene dehydration tower and a butadiene rectifying tower;
a discharge hole of the carbon four-material buffer tank is communicated with a feed inlet of the first rectifying tower through a pipeline, a discharge hole of the top of the first rectifying tower is communicated with a feed inlet of a reflux tank of the first rectifying tower through a pipeline, and a discharge hole of the bottom of the reflux tank of the first rectifying tower is communicated with a reflux hole of the first rectifying tower through a pipeline; the tower bottom discharge hole of the first rectifying tower is communicated with the feed inlet of the second rectifying tower through a pipeline; a discharge port at the top of the second rectifying tower is communicated with a feed port of a reflux tank of the second rectifying tower through a pipeline, and a discharge port at the bottom of the reflux tank of the second rectifying tower is communicated with a reflux port of the second rectifying tower through a pipeline; a discharge hole at the bottom of the second rectifying tower is communicated with a feed hole of the butene raw material buffer tank through a pipeline;
the butylene raw material buffer tank, the air compressor and the steam source are communicated with a feed inlet of the dehydrogenation reactor through pipelines, a discharge outlet of the dehydrogenation reactor is communicated with a feed inlet of the water-cooling acid washing tower through a pipeline, a discharge outlet of the water-cooling acid washing tower is communicated with a feed inlet of the compressor through a pipeline, a discharge outlet of the compressor is communicated with a feed inlet of the oil absorption tower through a pipeline, a discharge outlet of the oil absorption tower is communicated with a feed inlet of the absorption oil desorption tower through a pipeline, a discharge outlet of the absorption oil desorption tower is communicated with a feed inlet of the first extraction rectification tower through a pipeline, a discharge outlet of the first extraction rectification tower is communicated with a feed inlet of the second extraction rectification tower through a pipeline, a discharge outlet of the second extraction rectification tower is communicated with a feed inlet of the crude butadiene water washing tower through a pipeline, a discharge port at the top of the crude butadiene washing tower is communicated with a feed port of the butadiene dehydrating tower through a pipeline, and a discharge port at the bottom of the butadiene dehydrating tower is communicated with a feed port of the butadiene rectifying tower through a pipeline;
the device is characterized by further comprising a recovery rectifying tower, wherein a feed inlet of the recovery rectifying tower is communicated with a discharge outlet at the bottom of the butadiene dehydrating tower through a pipeline, and a discharge outlet at the bottom of the recovery rectifying tower is communicated with a butylene raw material buffer tank through a pipeline.
2. The integrated recovery system for purge gas and carbon four-residue in butadiene production according to claim 1, wherein the purge gas outlet of the reflux tank of the first rectification tower is communicated with the feed inlet of the recovery rectification tower.
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| CN201921567257.XU CN210595848U (en) | 2019-09-19 | 2019-09-19 | Purge gas and carbon four-residue comprehensive recovery system in butadiene production |
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| CN201921567257.XU CN210595848U (en) | 2019-09-19 | 2019-09-19 | Purge gas and carbon four-residue comprehensive recovery system in butadiene production |
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