CN203159507U - Aromatic hydrocarbon purifying device for coking crude benzene hydrofining - Google Patents
Aromatic hydrocarbon purifying device for coking crude benzene hydrofining Download PDFInfo
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- CN203159507U CN203159507U CN 201320165494 CN201320165494U CN203159507U CN 203159507 U CN203159507 U CN 203159507U CN 201320165494 CN201320165494 CN 201320165494 CN 201320165494 U CN201320165494 U CN 201320165494U CN 203159507 U CN203159507 U CN 203159507U
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Abstract
The utility model discloses an aromatic hydrocarbon purifying device for coking crude benzene hydrofining, which comprises an extraction rectifying tower, a liquid-liquid extraction tower, an aromatic hydrocarbon stripping tower, a crude benzene preheater, a hydrogenation oil preheater, a cooler, an air cooler, a raw material mixer, a discharged material mixer and a distributor, wherein the raw material mixer is connected with a lateral line of the extraction rectifying tower, the top of the extraction rectifying tower and a discharge lateral line of a rectifying section are connected with the discharged material mixer, the cooler is arranged behind the discharged material mixer and is connected with the feed port at the bottom of the liquid-liquid extraction tower, a discharge port at the bottom of the liquid-liquid extraction tower is connected with the top of the extraction rectifying tower, the bottom of the extraction rectifying tower is connected with the feed port of the aromatic hydrocarbon stripping tower, the distributor is connected at the bottom of the aromatic hydrocarbon stripping tower, and the distributor has two paths of outlets that are connected. According to the aromatic hydrocarbon purifying device, mass and heat are integrated, a comprehensive heat exchange network is optimized, and waste heat recovery is realized, so that the aromatic hydrocarbon separation effect is improved, and the operation cost is lowered.
Description
Technical field
The utility model belongs to petrochemical industry, relates to a kind of aromatic hydrocarbons purifying plant for hydrofining coking crude benzene, and this device is solvent with the N-N-formyl morpholine N-, separates purification aromatic hydrocarbons from aromatic hydrocarbons and non-aromatics mixture.
Background technology
Industrial solvent for the aromatic hydrocarbons extracting has N-N-formyl morpholine N-, tetramethylene sulfone and N-Methyl pyrrolidone etc. at present.N-N-formyl morpholine N-selectivity and solvability are good, and many remarkable advantages such as its corresponding extraction process has that solvent consumption is few, energy consumption is low, product purity and yield height are so use comparatively extensive.According to the unit operation feature, the aromatic hydrocarbons extracting can be divided into liquid-liquid extraction and extracting rectifying.Liquid-liquid extraction is the unit operation that utilizes stock liquid component dissolubility difference and realizing in solvent to separate, and is applicable to the reformate raw material that non-aromatics content is higher; Extracting rectifying is to change the stock blend relative volatility and realize the unit operation that separates being applicable to the hydrogenated oil raw material that aromatic hydrocarbons purity is higher by adding solvent.Use the method for liquid-liquid extraction, separating effect and the rate of recovery of aromatic hydrocarbons are relatively poor; Use the method for extracting rectifying, the solvent usage quantity is big, and energy consumption is higher.Liquid liquid extraction plant generally includes extraction tower, stripping tower, non-aromatics water wash column, recovery tower, water separation column etc.
The existing processes technology mainly contains following several:
Aromatic hydrocarbons extractive distillation SED (the Sulfolane Extractive Distillation) technology of petrochemical complex academy of sciences exploitation, the patent No. is CN1393507, chooses the tetramethylene sulfone double solvents, can obtain the aromatic hydrocarbons of higher degree, but its aromatic recovery rate is lower.And then exploitation N-N-formyl morpholine N-is the solvent arene extracting process, improved separating effect, but solvent load and energy consumption is bigger.
Some extracting rectifying arene extracting process have been developed in UHDE's application.US Patent No. Patent Number 4081355 discloses a kind of method that reclaims high purity aromatic hydrocarbons from contain aromatic hydrocarbons and non-aromatics mixture, raw material is gone through extraction tower, extractive distillation column, stripping tower, water separation column and is obtained high purity aromatic hydrocarbons, and solvent is the N-N-formyl morpholine N-.Many covering devices are at home and abroad gone into operation, and have created considerable economic benefit.US Patent No. Patent Number 6514387 discloses a kind of partition tower apparatus, and it assembles a partition tower with extractive distillation column, raw material recovery tower, has realized the integrated of quality and energy.
US Patent No. Patent Number 3944483, US Patent Number 4488936, US Patent Number 4776927 etc. all carry out associated description to the aromatic hydrocarbons extraction technique, and progressively to the prior art transformation, but all do not relate to according to component changes in distribution in the operating unit, and respond different separation method coupled configuration, and then improve aromatic hydrocarbons separating effect combination process.
The utility model content
The utility model provides the aromatic hydrocarbons purifying technique device that is used for hydrofining coking crude benzene, adopts N-N-formyl morpholine N-solvent, the method that is coupled by extracting rectifying and liquid-liquid extraction gas-liquid, thus improve the aromatic hydrocarbons separating effect, and reduce process cost.
In the coking crude benzene hydrogenation technique, aromaticity content is usually greater than 90% at the bottom of the preliminary fractionator, and this hydrogenated oil is not suitable for liquid-liquid extraction, but can take extracting rectifying.Extractive distillation column from the bottom of the tower to cat head, aromaticity content progressively reduces, especially rectifying section is formed the distribution abrupt change, its balance system is more suitable for liquid-liquid extraction to be separated.Therefore, extractive distillation column and liquid-liquid extraction tower gas-liquid are coupled in this technology, the extraction of extractive distillation column rectifying section side line gas phase, mix aromaticity content lower (less than 70%) in its component distribution of back with the cat head discharging, preferablyly take liquid-liquid extraction operation, enter that to be separated into rich aromatic hydrocarbons heavy phase behind the liquid-liquid extraction tower mutually light with poor aromatic hydrocarbons.Rich aromatic hydrocarbons heavy phase is introduced the extracting rectifying cat head again as backflow, and poor aromatic hydrocarbons gently is mainly non-aromatics in mutually, enters downstream section and handles.
This flow process adopts process system engineering methodology to realize that the mass-heat quantity set becomes, be coupled by extracting rectifying and liquid-liquid extraction gas-liquid, not only improve aromatic hydrocarbons and non-aromatics separating effect, improve aromatic recovery rate and purity simultaneously, and reduce solvent when condenser and reboiler.Simultaneously, the optimization synthesis heat exchanger network is realized that waste heat recovery, branch's aromatic hydrocarbons are carried and is heated up in a steamer lean solvent at the bottom of the tower, one preheating material crude benzol, and another is as extracting rectifying tower bottom reboiler thermal source, and then the preheating material hydrogenated oil, thereby reduces plant energy consumption.
The technical solution of the utility model is as follows:
The aromatic hydrocarbons purifying plant that is used for hydrofining coking crude benzene, comprising that extractive distillation column, liquid-liquid extraction tower, aromatic hydrocarbons are carried heats up in a steamer tower, crude benzol preheater, hydrogenated oil preheater, water cooler, air cooler, material mixer, goes out feed mixer and divider.Material mixer links to each other with the extractive distillation column side line, extracting rectifying top of tower and rectifying section discharging side line all with go out feed mixer and link to each other, be provided with water cooler after going out feed mixer, water cooler connects liquid-liquid extraction tower bottom opening for feed, liquid-liquid extraction tower bottom discharge port links to each other with the extracting rectifying top of tower again, extracting rectifying tower bottom and aromatic hydrocarbons are carried and are heated up in a steamer the tower opening for feed and link to each other, aromatic hydrocarbons is carried and is heated up in a steamer tower bottom connection divider, export distributor is divided into two-way and connects: after (1) connected the crude benzol preheater, the outlet of crude benzol preheater connected the liquid-liquid extraction top of tower again; (2) connect extractive distillation column reboiler, hydrogenated oil preheater, air cooler, material mixer successively by connection line.
Idiographic flow is:
(1) enters extractive distillation column after raw material hydrogenated oil and the heat exchange of lean solvent N-N-formyl morpholine N-, tower top pressure is 10-80kPa, theoretical balance progression is 25-50, solvent ratio is 4-8, the hydrogenated oil feed entrance point is the 8-12 level, and N-N-formyl morpholine N-feed entrance point is the 2-5 level, the place's side line gas phase extraction of rectifying section 1-5 level, the rich aromatic hydrocarbons heavy phase of liquid-liquid extraction tower enters the extracting rectifying cat head and crosses cold reflux, and double tower coupling reflux ratio is 0.5-0.9.
(2) after extractive distillation column ejects material and the gas phase side line mixes, be cooled to 30 ℃-50 ℃, enter at the bottom of the liquid-liquid extraction tower, liquid-liquid extraction tower counter-flow atmospheric operation, theoretical balance progression is 4-8, service temperature is 20 ℃-60 ℃, extraction agent is the N-N-formyl morpholine N-, and solvent ratio is 3-5.Extraction phase is respectively with extracting phase: be that the rich aromatic hydrocarbons heavy phase of solvent is mutually light with the poor aromatic hydrocarbons that is solvent with the non-aromatics with the N-N-formyl morpholine N-.Wherein rich aromatic hydrocarbons heavy phase enters the extracting rectifying cat head, crosses cold reflux as rectifying section, and poor aromatic hydrocarbons gently is mainly non-aromatics in mutually, enters downstream section and handles.
(3) consist of N-N-formyl morpholine N-and aromatic hydrocarbons at the bottom of the extractive distillation column, rich solvent enters aromatic hydrocarbons and carries and heat up in a steamer tower and separate.Aromatic hydrocarbons is carried and is heated up in a steamer the tower vacuum operating, and theoretical balance progression is 10-20, and reflux ratio is 0.5-1, and the rich solvent feed entrance point is the 4-7 level.Cat head obtains pure aromatics, is that lean solvent N-N-formyl morpholine N-recycles at the bottom of the tower.
(4) lean solvent N-N-formyl morpholine N-is divided into the two-way circulation, and allocation proportion is 1:8-10, introduces the liquid-liquid extraction tower after the one heat exchange, returns extractive distillation column after another heat exchange.The N-N-formyl morpholine N-has small loss in the working cycle, replenishes a small amount of novel solvent at the extracting rectifying cat head.
Compare with existing flow process, aromatic hydrocarbons purity of the present utility model reaches more than 99.7%, and the rate of recovery reaches more than 99.9%.Solvent ratio reduces more than 10%, and cold and hot general facilities consumption reduces, and recovery of heat increases more than 7%.
Description of drawings
Accompanying drawing is aromatic hydrocarbons extractor structural representation.
Among the figure: 1 air cooler; 2 hydrogenated oil preheaters; 3 material mixers; 4 extractive distillation columns; 5 reboilers; 6 go out feed mixer; 7 water coolers; 8 liquid-liquid extraction towers; 9 aromatic hydrocarbons are carried and are heated up in a steamer tower; 10 dividers; 11 crude benzol preheaters.
Embodiment
Below in conjunction with technical scheme and accompanying drawing, be described in detail embodiment of the present utility model.
As shown in drawings, material mixer 3 links to each other with extractive distillation column 4 side lines, extractive distillation column 4 tops and rectifying section discharging side line with go out feed mixer 6 and link to each other, be provided with water cooler 7 after going out feed mixer 6, water cooler 7 connects liquid-liquid extraction tower 8 bottom feed mouths, liquid-liquid extraction tower 8 bottom discharge mouths link to each other with extractive distillation column 4 tops again, extractive distillation column 4 bottoms and aromatic hydrocarbons are carried and are heated up in a steamer tower 9 opening for feeds and link to each other, aromatic hydrocarbons is carried and is heated up in a steamer tower 9 bottoms connection divider 10, divider 10 outlets are divided into two-way and connect: one, after connecting crude benzol preheater 11,11 outlets of crude benzol preheater connect liquid-liquid extraction tower 8 tops again; Its two, connect extractive distillation column reboiler 5, hydrogenated oil preheater 2, air cooler 1, material mixer 3 successively by connection line.
Detailed process is:
As shown in drawings, raw material hydrogenated oil temperature is 87.7 ℃, and mass rate is 5457.4 kg/h.After hydrogenated oil preheater 2 and lean solvent heat exchange, temperature reaches 98.8 ℃, enters extractive distillation column 4 again, and pressure is 55kPa, and tower top temperature is 72.83 ℃, and column bottom temperature is 150.8 ℃.The extraction of rectifying section side line gas phase, flow is 408.27 kg/h.
Cat head discharging and side line mix through going out feed mixer 6, are cooled to 40 ℃ by water cooler 7 again, enter at the bottom of liquid-liquid extraction tower 8 towers.Extraction tower is the normal pressure counter-current operation, and extraction agent is the N-N-formyl morpholine N-.Extraction phase is respectively with extracting phase: rich aromatic hydrocarbons heavy phase is mutually light with poor aromatic hydrocarbons.Rich aromatic hydrocarbons heavy phase is mainly aromatic hydrocarbons and N-N-formyl morpholine N-, reenters extractive distillation column 4 cats head, crosses cold reflux.The light phase mass rate of poor aromatic hydrocarbons is 183kg/h, and non-aromatics content is more than 97%.
Rich solvent enters aromatic hydrocarbons and carries and heat up in a steamer tower 9, and tower top pressure is-39kPa, and tower top temperature is 54.7 ℃, and column bottom temperature is 206.9 ℃.Cat head obtains pure aromatics, and mass rate is 5267.8kg/h, is lean solvent N-N-formyl morpholine N-at the bottom of the tower, and mass rate is 34704kg/h.
Lean solvent N-N-formyl morpholine N-is divided into the two-way circulation through divider 10, one enters crude benzol preheater 11 preheating material crude benzol, introduce liquid-liquid extraction tower 8 again, another is as extractive distillation column tower bottom reboiler 5 thermals source, enter hydrogenated oil preheater 2 preheating hydrogenated oils again, be cooled to 120 ℃ finally by air cooler 1, enter extractive distillation column.The N-N-formyl morpholine N-has small loss in the working cycle, replenishes a small amount of novel solvent at the extracting rectifying cat head.
Claims (1)
1. aromatic hydrocarbons purifying plant that is used for hydrofining coking crude benzene, comprising that extractive distillation column, liquid-liquid extraction tower, aromatic hydrocarbons are carried heats up in a steamer tower, crude benzol preheater, hydrogenated oil preheater, water cooler, air cooler, material mixer, goes out feed mixer and divider; Material mixer links to each other with the extractive distillation column side line, extracting rectifying top of tower and rectifying section discharging side line all with go out feed mixer and link to each other, be provided with water cooler after going out feed mixer, water cooler connects liquid-liquid extraction tower bottom opening for feed, liquid-liquid extraction tower bottom discharge port links to each other with the extracting rectifying top of tower again, extracting rectifying tower bottom and aromatic hydrocarbons are carried and are heated up in a steamer the tower opening for feed and link to each other, aromatic hydrocarbons is carried and is heated up in a steamer tower bottom connection divider, export distributor is divided into two-way and connects: after (1) connected the crude benzol preheater, the outlet of crude benzol preheater connected the liquid-liquid extraction top of tower again; (2) connect extractive distillation column reboiler, hydrogenated oil preheater, air cooler, material mixer successively by connection line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320165494 CN203159507U (en) | 2013-04-05 | 2013-04-05 | Aromatic hydrocarbon purifying device for coking crude benzene hydrofining |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201320165494 CN203159507U (en) | 2013-04-05 | 2013-04-05 | Aromatic hydrocarbon purifying device for coking crude benzene hydrofining |
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| CN203159507U true CN203159507U (en) | 2013-08-28 |
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| CN 201320165494 Expired - Fee Related CN203159507U (en) | 2013-04-05 | 2013-04-05 | Aromatic hydrocarbon purifying device for coking crude benzene hydrofining |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130828 Termination date: 20150405 |
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