CN104745224A - Waste heat recycling device and recycling process - Google Patents
Waste heat recycling device and recycling process Download PDFInfo
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- CN104745224A CN104745224A CN201510102815.5A CN201510102815A CN104745224A CN 104745224 A CN104745224 A CN 104745224A CN 201510102815 A CN201510102815 A CN 201510102815A CN 104745224 A CN104745224 A CN 104745224A
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- depentanizer
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Abstract
The invention discloses a waste heat recycling device and recycling process. The waste heat recycling device mainly comprises a raw material buffer tank, a charge/discharge heat exchanger of a depentanizer, a depentanizer and an octane removal tower, wherein the raw material tank is connected with the octane removal tower through a shell pass of the charge/discharge heat exchanger of the depentanizer; the tower bottom of the octane removal tower is connected with the shell pass of the charge/discharge heat exchanger of the depentanizer through a bottom pump of the octane removal tower; a tube pass outlet of the charge/discharge heat exchanger of the depentanizer extends outwards after passing through an air cooler; the depentanizer is connected with the octane removal tower through the bottom pump of the depentanizer; the tower top of the octane removal tower is connected with a buffer tank through the air cooler; the buffer tank is connected with an aromatic hydrocarbon extracting unit. The depentanizer disclosed by the invention replaces an aromatization fractionation and cutting tower to perform fractionation and cut reorganized mixed aromatic hydrocarbon raw material, so that the process of the aromatic hydrocarbon extracting device is greatly simplified, the tower-bottom substrate of the octane removal tower is utilized to exchange heat with the charged material of the depentanizer, the charge temperature of the depentanizer and the octane removal tower is increased, and the steam consumption is reduced.
Description
Technical field
The present invention relates to aromatic extraction unit heat recovery technology field, be specifically related to a kind of waste-heat recovery device and recovery process thereof.
Background technology
Aromatic extraction unit is the downstream unit of gasoline reformer, and its raw material is reformation BTX aromatics and crude benzol BTX aromatics C, through Sulfolane Extraction and precision fractional distillation technique, produces Benzene and Toluene, to meet the industrial needs such as plastics, rubber, food-processing.
Existing aromatic extraction unit is made up of feed material preparation units and Aromatics Extractive Project unit, wherein feed material preparation units comprises aromizing fractionation Cutting Tap, depentanizer and de-octane tower, reformation BTX aromatics is first cut through aromizing fractionation Cutting Tap, and then through the process of depentanizer and de-octane tower, finally deliver to extraction tower process, de-octane bottom product outside tank sending district time temperature at 145-150 DEG C, flow is about 15t/h, send outside in process and directly rely on air cooling to carry out cooling process, waste a large amount of heat energy, and reformation BTX aromatics raw material also will first through the process of aromizing fractionation Cutting Tap, flow process comparatively complexity cause facility investment and running cost higher.
Summary of the invention
The invention provides a kind of waste-heat recovery device and recovery process thereof, with the problem of the Aromatics Extractive Project pretreatment unit thermal waste and flow process complexity that solve prior art existence.
The technical solution adopted for the present invention to solve the technical problems is:
A kind of waste-heat recovery device, primarily of raw material surge tank, depentanizer entry/exit material interchanger, depentanizer and de-octane tower composition, raw material surge tank is connected with depentanizer by the shell side of depentanizer entry/exit material interchanger, be connected with the tube side of depentanizer entry/exit material interchanger by de-octane column bottoms pump at the bottom of the tower of de-octane tower, the tube side outlet of depentanizer entry/exit material interchanger is sent outside after air-cooler, depentanizer is connected with de-octane tower by depentanize column bottoms pump, de-octane column overhead is connected with surge tank by air-cooler, surge tank is connected with Aromatics Extractive Project unit.
The recovery process of above-mentioned waste-heat recovery device, aromizing fractionation Cutting Tap is replaced to carry out fractionation cutting to reformation BTX aromatics raw material by de-octane tower, de-octane tower materials at bottom of tower is utilized to carry out heat exchange to depentanizer charging, improve the feeding temperature of depentanizer and de-octane tower, reduce steam consumption, concrete technology step is: reformation BTX aromatics raw material is delivered in the shell side of depentanizer entry/exit material interchanger by raw material surge tank through depentanizer fresh feed pump, reformation BTX aromatics raw material carries out heat exchange with the de-octane tower materials at bottom of tower in tube side in depentanizer entry/exit material interchanger, depentanizer feeding temperature is carried to 80 DEG C by 52 DEG C, material at the bottom of depentanizer is by being pumped in de-octane tower at the bottom of depentanizer, de-octane tower materials at bottom of tower is delivered in the tube side of depentanizer entry/exit material interchanger through de-octane column bottoms pump, after heat exchange, finally irrigated area is delivered to again through air-cooler, de-octane column overhead material is after air-cooler cooling, Aromatics Extractive Project unit is delivered to through surge tank.
Present invention achieves reformation BTX aromatics raw material directly to extraction plant charging, no longer by aromizing fractionation Cutting Tap, not only save the steam consumption of aromizing fractionation Cutting Tap, simultaneously by the transformation to de-octane tower tower bottom flow journey, after utilizing depentanizer entry/exit material interchanger to reclaim heat energy fully, depentanizer feeding temperature is carried to 80 DEG C by 52 DEG C, de-octane tower feeding temperature is carried to 120 DEG C by 70 DEG C, demarcate according to actual production, device middle pressure steam consumption reduces 4.35t/h, low-pressure steam consumption increases 1.13t/h, total can steam saving consumption (4.35t/h-1.13t/h)=3.22t/h, reduce plant energy consumption and be about 9.5kg mark oil/ton
The present invention replaces aromizing fractionation Cutting Tap to carry out fractionation cutting to reformation BTX aromatics raw material by taking off octane tower, not only enormously simplify the technical process of aromatic extraction unit, and utilize de-octane tower materials at bottom of tower to carry out heat exchange to depentanizer charging, improve the feeding temperature of depentanizer and de-octane tower, reduce steam consumption.
accompanying drawing illustrates:
Below in conjunction with drawings and Examples, the present invention is further described.
Fig. 1 is the structural representation of apparatus of the present invention.
1 raw material surge tank, 2 depentanizer fresh feed pumps, 3 depentanizer entry/exit material interchanger, 4 depentanizers, 5 de-octane towers, 6 depentanize column bottoms pumps, 7 de-octane column bottoms pump, 8 air-coolers, 9 air-coolers, 10 surge tanks, 11 Aromatics Extractive Project unit in figure.
embodiment:
As shown in the figure, a kind of waste-heat recovery device, primarily of raw material surge tank 1, depentanizer entry/exit material interchanger 3, depentanizer 4 and de-octane tower 5 form, raw material surge tank 1 is connected with depentanizer 4 by the shell side of depentanizer entry/exit material interchanger 3, be connected with the tube side of depentanizer entry/exit material interchanger 3 by de-octane column bottoms pump 7 at the bottom of the tower of de-octane tower 5, the tube side outlet of depentanizer entry/exit material interchanger 3 is sent outside after air-cooler 8, depentanizer 4 is connected with de-octane tower 5 by depentanize column bottoms pump 6, de-octane tower 5 tower top is connected with surge tank 10 by air-cooler 9, surge tank 10 is connected with Aromatics Extractive Project unit 11.
The recovery process of above-mentioned waste-heat recovery device, aromizing fractionation Cutting Tap is replaced to carry out fractionation cutting to reformation BTX aromatics raw material by de-octane tower, de-octane tower materials at bottom of tower is utilized to carry out heat exchange to depentanizer charging, improve the feeding temperature of depentanizer and de-octane tower, reduce steam consumption, concrete technology step is: reformation BTX aromatics raw material is delivered in the shell side of depentanizer entry/exit material interchanger 3 by raw material surge tank 1 through depentanizer fresh feed pump 2, reformation BTX aromatics raw material carries out heat exchange with the de-octane tower materials at bottom of tower in tube side in depentanizer entry/exit material interchanger 3, depentanizer 4 feeding temperature is carried to 80 DEG C by 52 DEG C, material at the bottom of depentanizer is delivered in de-octane tower 5 by depentanize column bottoms pump 6, de-octane tower 5 materials at bottom of tower is delivered in the tube side of depentanizer entry/exit material interchanger 3 through de-octane column bottoms pump 7, after heat exchange, finally irrigated area is delivered to again through air-cooler 8, de-octane column overhead material is after air-cooler 9 cools, Aromatics Extractive Project unit 11 is delivered to through surge tank 10.
Claims (2)
1. a waste-heat recovery device, it is characterized in that primarily of raw material surge tank, depentanizer entry/exit material interchanger, depentanizer and de-octane tower composition, raw material surge tank is connected with depentanizer by the shell side of depentanizer entry/exit material interchanger, be connected with the tube side of depentanizer entry/exit material interchanger by de-octane column bottoms pump at the bottom of the tower of de-octane tower, the tube side outlet of depentanizer entry/exit material interchanger is sent outside after air-cooler, depentanizer is connected with de-octane tower by depentanize column bottoms pump, de-octane column overhead is connected with surge tank by air-cooler, surge tank is connected with Aromatics Extractive Project unit.
2. the recovery process of waste-heat recovery device according to claim 1, it is characterized in that replacing aromizing fractionation Cutting Tap to carry out fractionation cutting to reformation BTX aromatics raw material by de-octane tower, de-octane tower materials at bottom of tower is utilized to carry out heat exchange to depentanizer charging, concrete technology step is that reformation BTX aromatics raw material is delivered in the shell side of depentanizer entry/exit material interchanger by raw material surge tank through depentanizer fresh feed pump, reformation BTX aromatics raw material carries out heat exchange with the de-octane tower materials at bottom of tower in tube side in depentanizer entry/exit material interchanger, depentanizer feeding temperature is carried to 80 DEG C by 52 DEG C, material at the bottom of depentanizer is by being pumped in de-octane tower at the bottom of depentanizer, de-octane tower materials at bottom of tower is delivered in the tube side of depentanizer entry/exit material interchanger through de-octane column bottoms pump, after heat exchange, finally irrigated area is delivered to again through air-cooler, de-octane column overhead material is after air-cooler cooling, Aromatics Extractive Project unit is delivered to through surge tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510102815.5A CN104745224A (en) | 2015-03-10 | 2015-03-10 | Waste heat recycling device and recycling process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510102815.5A CN104745224A (en) | 2015-03-10 | 2015-03-10 | Waste heat recycling device and recycling process |
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| Publication Number | Publication Date |
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| CN104745224A true CN104745224A (en) | 2015-07-01 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201510102815.5A Pending CN104745224A (en) | 2015-03-10 | 2015-03-10 | Waste heat recycling device and recycling process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2018535279A (en) * | 2015-08-24 | 2018-11-29 | サウジ アラビアン オイル カンパニー | Recovery and reuse of waste energy in industrial facilities |
Citations (3)
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| CN1260341A (en) * | 1999-05-28 | 2000-07-19 | 中国石油化工集团公司 | Method for separating arene from hydrocarbons mixture by use of extraction and rectification |
| CN101091835A (en) * | 2006-06-22 | 2007-12-26 | 中国石油化工股份有限公司 | Extractive distillation method with heat exchange through parallel connection |
| CN204474605U (en) * | 2015-03-10 | 2015-07-15 | 河北新启元能源技术开发股份有限公司 | Waste-heat recovery device |
-
2015
- 2015-03-10 CN CN201510102815.5A patent/CN104745224A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1260341A (en) * | 1999-05-28 | 2000-07-19 | 中国石油化工集团公司 | Method for separating arene from hydrocarbons mixture by use of extraction and rectification |
| CN101091835A (en) * | 2006-06-22 | 2007-12-26 | 中国石油化工股份有限公司 | Extractive distillation method with heat exchange through parallel connection |
| CN204474605U (en) * | 2015-03-10 | 2015-07-15 | 河北新启元能源技术开发股份有限公司 | Waste-heat recovery device |
Non-Patent Citations (4)
| Title |
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| 奚俊 等: "苯抽提装置现状分析及节能措施", 《化学工程》 * |
| 李俊奎 等: "0.1Mt/a苯抽提换热流程优化", 《科技创新导报》 * |
| 李成栋: "《催化重整装置操作指南》", 31 January 2000 * |
| 陆良福: "《石油化工技工学校统编教材 炼油过程及设备》", 31 May 1993 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2018535279A (en) * | 2015-08-24 | 2018-11-29 | サウジ アラビアン オイル カンパニー | Recovery and reuse of waste energy in industrial facilities |
| JP2018535278A (en) * | 2015-08-24 | 2018-11-29 | サウジ アラビアン オイル カンパニー | Recovery and reuse of waste energy in industrial facilities |
| JP2018536035A (en) * | 2015-08-24 | 2018-12-06 | サウジ アラビアン オイル カンパニー | Recovery and reuse of waste energy in industrial facilities |
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