CN104673353B - A kind of method of recovered ethylene device quenching oil heat - Google Patents
A kind of method of recovered ethylene device quenching oil heat Download PDFInfo
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- CN104673353B CN104673353B CN201510073000.9A CN201510073000A CN104673353B CN 104673353 B CN104673353 B CN 104673353B CN 201510073000 A CN201510073000 A CN 201510073000A CN 104673353 B CN104673353 B CN 104673353B
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- 238000010791 quenching Methods 0.000 title claims abstract description 52
- 230000000171 quenching effect Effects 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims abstract description 35
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 13
- 239000005977 Ethylene Substances 0.000 title claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 44
- 239000000203 mixture Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000003809 water extraction Methods 0.000 claims description 3
- 238000004364 calculation method Methods 0.000 claims description 2
- 239000007791 liquid phase Substances 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 239000003921 oil Substances 0.000 abstract description 48
- 238000011084 recovery Methods 0.000 abstract description 7
- 238000010790 dilution Methods 0.000 abstract description 6
- 239000012895 dilution Substances 0.000 abstract description 6
- 238000007634 remodeling Methods 0.000 abstract description 3
- 239000000295 fuel oil Substances 0.000 abstract description 2
- 238000000197 pyrolysis Methods 0.000 abstract description 2
- 238000005728 strengthening Methods 0.000 abstract 1
- 230000009466 transformation Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of method for recovered ethylene device quenching oil heat.Traditional quenching oil heat recuperation flow process is generally that quenching oil is divided into two-way, and a road is as the charging of Pyrolysis fuel oil PFO stripping tower; Another road is as the thermal source of Dilution steam generator, and the quenching oil after heat exchange is injected into cracked oil gas pipeline after pyrolyzer, returns main fractionating tower after mixing with cracked oil.In traditional process, quenching oil is as after Dilution steam generator thermal source, and with regard to high-temperature oil gas mixing after direct and pyrolyzer, heat is not fully reclaimed.Remodeling method of the present invention comprises: (1) water preheater on existing drum is connected a preheater, and the heat exchange of water and quenching oil on strengthening drum, to improve water temp on drum; (2) at the bottom of process water stripper tower, increasing reboiler newly or being replaced by existing reboiler with quenching oil is the reboiler of thermal source.This remodeling method can the superfluous heat of efficient recovery quenching oil, and reduce energy wastage, and workload is little, expense is low.
Description
Technical field
The present invention relates to a kind of method of recovered ethylene device quenching oil heat.
Background technology
The charging of ethylene unit main fractionating tower is splitting gas, and the part oil of oil at the bottom of its tower after its heat is reclaimed in heat exchange mixes with splitting gas, splitting gas is had to the effect of cooling fast, therefore also referred to as quenching oil.At the bottom of tower, the traditional process of oil is generally divided into two-way, and a road is as the charging of Pyrolysis fuel oil PFO stripping tower; Another road, as the thermal source of Dilution steam generator, returns main fractionating tower with cracking air-fuel mixture afterwards.Utilize quenching oil at the bottom of ethene main fractionating tower tower to be the main path of oil heat at the bottom of recovery tower on ethylene industry as the thermal source of Dilution steam generator system, for there is low-pressure steam (0.2-0.8MPaG), this heat recovery system is made up of multiple stage interchanger.
In traditional process, quenching oil, as after Dilution steam generator thermal source, just directly and after pyrolyzer returns main fractionating tower after high-temperature oil gas mixing, and the recovery of heat is abundant not, causes the waste of energy.
Summary of the invention
The object of the present invention is to provide a kind of can the method for recovered ethylene device quenching oil heat further.The method overcomes the insufficient process defect of traditional technology heat recuperation, and in original flow process, newly-increased interchanger, can reach the object reclaiming quenching oil net heat further.
The method of the recovered ethylene device quenching oil heat that the present invention proposes, at the bottom of described existing ethylene unit main fractionating tower tower, the recovery method of quenching oil heat is, the quenching oil that main fractionating tower 1 produces is sent after pipeline flows out from quenching oil at the bottom of tower, be divided into two-way, one tunnel mix with main fractionating tower feeding gas laggard enter main fractionating tower, second tunnel is first as the thermal source of vapour generator, and the upper water preheater then entering this vapour generator from the quenching oil after the interchanger outflow of vapour generator is water extraction supplying heat source drum; For reclaiming the heat of quenching oil further, water preheater on newly-increased drum on existing remodeling method, and at the bottom of process water stripper tower, to increase reboiler newly or be replaced by original reboiler with quenching oil be the reboiler of thermal source, concrete steps are as follows:
(1) water preheater on newly-increased drum
On original drum, on water preheater 5, series connection increases water preheater 6 on drum newly, and on described newly-increased drum, the heat interchanging area of every platform interchanger of water preheater 6 is 50-2000 square metre; In actually operating, by regulating the quenching oil flow entering water preheater 6 on water preheater 5 and newly-increased drum on original drum, to guarantee on drum water temp close to or reach bubble point temperature;
(2) at the bottom of process water stripper tower, increasing reboiler newly or being replaced by original reboiler with quenching oil is the reboiler of thermal source
The superfluous heat that quenching oil on newly-increased drum described in further recycling step (1) after water preheater 6 outflow produces, be specially: newly-increased reboiler 9 is set bottom process water stripper 7, quenching oil is delivered at the bottom of the tower of process water stripper 7, then newly-increased reboiler 9 is entered, to substitute the low-pressure steam of original reboiler 8; Described newly-increased reboiler 9 is 1-2 platform; In order to reduce the investment of interchanger 9, or quenching oil is accessed original reboiler 8 simultaneously, described newly-increased reboiler 9 type selecting is determined according to liquid phase flow rate calculation at the bottom of quenching oil and stripping tower tower, and the heat interchanging area of every platform interchanger of newly-increased reboiler 9 is 50-2000 square metre;
(3) step (1) and step (2) can be implemented separately, also can implement simultaneously.
Beneficial effect of the present invention is: the inventive method can the superfluous heat of efficient recovery quenching oil, and reduce energy wastage, and workload is little, expense is low.
Accompanying drawing explanation
Fig. 1 is transformation and optimization schema.Wherein thickened portion is flow process newly-increased after transformation.
Number in the figure: 1 is main fractionating tower, 2 is that at the bottom of tower, pipeline sent by quenching oil, and 3 is vapour generator, 4 is quenching oil return line, and 5 is water preheater on original drum, and 6 is water preheater on newly-increased drum, 7 is process water stripper, and 8 is original reboiler, and 9 is newly-increased reboiler.
Embodiment
By reference to the accompanying drawings technical scheme of the present invention is described in further detail below by embodiment.
Embodiment 1: certain 800,000 tons of ethylene unit quenching oil heat recovery system transformation.
Original heat recuperation flow process as shown in Figure 1, after quenching oil at the bottom of tower in the main fractionating tower 1 of ethylene unit sends pipeline 2 extraction by quenching oil at the bottom of tower, quenching oil tower exit temperature at the bottom of tower is 210 DEG C, two-way is divided into after going out tower, one tunnel directly returns main fractionating tower 1 hypomere, another road then by water preheater 5 on original drum to water extraction supplying heat source on drum, it is 180 DEG C that oil at the bottom of described tower returns tower temperature.
Improved heat recuperation flow process is as shown in Fig. 1 thickened portion: water preheater 6 on the rear newly-increased drum of connecting of (1) water preheater 5 on original drum, by regulating the quenching oil flow entering water preheater 6 on water preheater 5 and newly-increased drum on original drum, to guarantee on drum water temp close to or reach bubble point temperature.(2) a newly-increased reboiler 9 is set up, using quenching oil as heating medium.Increase the heat exchange process of quenching oil to original reboiler 8 of process water stripper 7, substitute the low-pressure steam that original reboiler 8 used originally.
After above-mentioned transformation completes, quenching oil returns tower temperature and is reduced to 170 DEG C by original 180 DEG C, the heat reclaimed improves the upper water temp of drum on the one hand, dilution steam generation drum steam production is improved, on the other hand can the heating steam of alternative techniques water stripper, volume increase and the steam 25t/h altogether saved.Steam price according to 130 yuan/ton, year energy-saving benefit reach 2,730 ten thousand yuan/year.
Claims (1)
1. the method for a recovered ethylene device quenching oil heat, being the quenching oil that produces of main fractionating tower (1) sends after pipeline flows out from quenching oil at the bottom of tower, be divided into two-way, one tunnel mix with main fractionating tower feeding gas laggard enter main fractionating tower, second tunnel is first as the thermal source of vapour generator, and the upper water preheater then entering this vapour generator from the quenching oil after the interchanger outflow of vapour generator is water extraction supplying heat source drum; It is characterized in that the heat for reclaiming quenching oil further, water preheater on a newly-increased drum in existing design or the device that run, and to increase reboiler newly or be replaced by original reboiler with quenching oil at the bottom of process water stripper tower be the reboiler of thermal source, concrete steps are as follows:
(1) water preheater on newly-increased drum
Water preheater (6) on the newly-increased drum of the upper series connection of water preheater (5) on original drum, on described newly-increased drum, the heat interchanging area of every platform interchanger of water preheater (6) is 50-2000 square metre; In actually operating, by regulating the quenching oil flow entering water preheater (6) on water preheater (5) and newly-increased drum on original drum, to guarantee on drum that water temp is close or reach bubble point temperature;
(2) at the bottom of process water stripper tower, increasing reboiler newly or being replaced by original reboiler with quenching oil is the reboiler of thermal source
Superfluous heat contained in quenching oil on newly-increased drum described in further recycling step (1) after water preheater (6) outflow, be specially: in process water stripper (7) bottom, newly-increased reboiler (9) is set, quenching oil is delivered at the bottom of the tower of process water stripper (7), then newly-increased reboiler (9) is entered, to substitute the low-pressure steam of original reboiler (8); Described newly-increased reboiler (9) is 1-2 platform; In order to reduce number of units or the investment of interchanger (9), or quenching oil is accessed original reboiler (8) simultaneously, described newly-increased reboiler (9) type selecting is determined according to liquid phase flow rate calculation at the bottom of quenching oil and stripping tower tower, and the heat interchanging area of every platform interchanger of newly-increased reboiler (9) is 50-2000 square metre.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510073000.9A CN104673353B (en) | 2015-02-12 | 2015-02-12 | A kind of method of recovered ethylene device quenching oil heat |
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| CN201510073000.9A CN104673353B (en) | 2015-02-12 | 2015-02-12 | A kind of method of recovered ethylene device quenching oil heat |
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| CN104673353A CN104673353A (en) | 2015-06-03 |
| CN104673353B true CN104673353B (en) | 2016-01-27 |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105838411B (en) * | 2016-03-23 | 2017-10-10 | 中国石油化工股份有限公司 | The Auxiliary Processing Unit and processing method of ethylene unit chilling system in petrochemical industry |
| CN106016794B (en) * | 2016-05-20 | 2019-02-19 | 上海优华系统集成技术股份有限公司 | A kind of aromatic device waste heat recycling system and method |
| CN114835550B (en) * | 2021-02-02 | 2023-04-18 | 中国石油化工股份有限公司 | Pyrolysis gas waste heat recovery device and method |
| CN114836239B (en) * | 2021-02-02 | 2023-04-18 | 中国石油化工股份有限公司 | Device and method for recovering heat of pyrolysis gas and removing heavy components |
| CN114836238B (en) * | 2021-02-02 | 2023-04-07 | 中国石油化工股份有限公司 | Device and method for increasing kettle temperature of gasoline fractionating tower |
| CN114836237B (en) * | 2021-02-02 | 2023-04-11 | 中国石油化工股份有限公司 | Pyrolysis gas heat recovery device and method for reducing diameter of gasoline fractionating tower |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101323553A (en) * | 2007-06-13 | 2008-12-17 | 中国石油天然气股份有限公司 | Method for increasing temperature of ethylene unit quenching oil tower bottom |
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| US8044254B2 (en) * | 2007-09-27 | 2011-10-25 | Uop Llc | Process for enhanced olefin production |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101323553A (en) * | 2007-06-13 | 2008-12-17 | 中国石油天然气股份有限公司 | Method for increasing temperature of ethylene unit quenching oil tower bottom |
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Effective date of registration: 20180413 Address after: 201206 24A1 room 58, new Golden Bridge Road, China (Shanghai) free trade zone Patentee after: Shanghai Huide Energy Integration Technology Co., Ltd. Address before: 201206 room 913, new Jinqiao Road, Pudong, Pudong New Area, Shanghai, 913 Patentee before: Zhang Gaobo |