CN103131472A - Process method for delaying coking apparatus fractionation tower online salt washing - Google Patents
Process method for delaying coking apparatus fractionation tower online salt washing Download PDFInfo
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- CN103131472A CN103131472A CN2011103802871A CN201110380287A CN103131472A CN 103131472 A CN103131472 A CN 103131472A CN 2011103802871 A CN2011103802871 A CN 2011103802871A CN 201110380287 A CN201110380287 A CN 201110380287A CN 103131472 A CN103131472 A CN 103131472A
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Abstract
The present invention relates to a process method for delaying coking apparatus fractionation tower online salt washing. The method comprises that: an adjustment valve A is closed, an adjustment valve B is opened, and a gas phase temperature of the lower portion of a top circulation oil collection tank is controlled to more than 130 DEG C; fractionation tower top three separator sewage containing sulfur enters the fractionation tower through a top circulation oil return-to-tower pipeline, washes salts and scales on tower trays, then enters the top circulation oil collection tank, is subjected to pressure increase through a top circulation oil pump B, and then enters a fractionation tower top air cooler to be washed; the washed oil-water mixture enters the fractionation tower top three separator, part of the separated gasoline returns to the fractionation tower and part of the separated gasoline is discharged out of the apparatus with a gasoline cold reflux pipeline, and the sewage containing sulfur enters a downstream acid water steam stripping device; when a color of the sewage containing sulfur is not changed, the purified water enters the fractionation tower through the top circulation oil return-to-tower pipeline and enters the fractionation tower top air cooler; and the washed oil-water mixture enters the fractionation tower top three separator to carry out oil water separation. The method has characteristics of safety and environmental protection, wherein externally discharge amounts of salt sewage and oil sewage are reduced, and long-term operation requirements of the apparatus can be met.
Description
Technical field
The present invention relates to the processing method of the online desalinization of soil by flooding or leaching of a kind of delayed coker fractionator, belong to the refining of petroleum field.
Background technology
Delayed coking unit is a kind of degree of depth thermocracking process that mink cell focus is converted into to dry gas, liquefied gas, coker gasoline, coker gas oil, wax tailings and coke, and raw material is generally the vacuum residuum that the upstream atmospheric and vacuum distillation unit comes.Because organic chloride in coking raw material and nitride can not thoroughly be removed in the electric desalting process, after the atmospheric and vacuum distillation unit deep drawing, this part material mainly concentrates in vacuum residuum, when vacuum residuum is heated to 500 ℃ while entering coke drum through process furnace, under the hot environments of atom in coke drum such as the N in residual oil, Cl, H, O, reaction generates N
2, NH
3, O
2deng product, simultaneously in residual oil, the heat absorption hydrolysis reaction occurs and generates HCl in organic chloride and butter in coke drum, due to the oil gas of generation by NH
3be carried to rapidly in separation column with HCl, make building-up reactions and hydrolysis reaction in coke drum constantly carry out, thereby produce a large amount of NH
3and HCl.In separation column, NH
3with HCl, combination at suitable temperature generates NH
4cl, NH
4cl is carried into the top tower tray with minimum particle form.Tiny NH
4the Cl particle, on the top of separation column, is dissolved in topical hypothermia's water, due to NH
4the boiling point of Cl solution is far above the boiling point of water, it is in the decline reflux course, because being distillated, the rising gradually of temperature is condensed into a kind of full-bodied semi-fluid, this semi-fluid and iron rust, coke powder etc. mix and are deposited on tower tray, return wire, downtake and seal pot etc. and locate, run up to the proper flow that to a certain degree will hinder liquid, stop up the perforate on tower tray, cause the separation column pressure drop to increase gradually, thereby cause separation column to rush that tower, diesel oil pump are found time, gasoline endpoint is too high.As this part NH
4when the Cl particle is fractionated overhead product and is carried to separation column head space cooler, easily salt crust in the tube bank of separation column head space cooler, cause separation column head space cooler cooling performance to descend, and had a strong impact on the safety in production of whole device.
Summary of the invention
The processing method that the purpose of this invention is to provide the online desalinization of soil by flooding or leaching of a kind of delayed coking unit separation column; It is the processing method that has a kind of online desalinization of soil by flooding or leaching of the problem exploitations such as fractionation tower top and separation column head space cooler salt crust for current delayed coking unit.This technology characteristics is that desalinization of soil by flooding or leaching process is divided into dirty washing and two processes of washing, and can in the situation that device do not stop work, do not affect quality product, outer get rid of sump oil to fractionation tower top top follow tower tray, system is followed on top and separation column head space cooler system is washed online, perfect existing delayed coking flow process.This safe in process environmental protection, reduced the outer amount of getting rid of of online desalinization of soil by flooding or leaching sump oil sewage, can meet the requirement of the long-term operation of delayed coking unit.
The present invention is the processing method of the online desalinization of soil by flooding or leaching of a kind of delayed coking unit separation column, and its technical scheme adopted is:
The setting device treatment capacity.The treatment capacity that slowly reduces each branch of process furnace, to zone of reasonableness, is adjusted fire box temperature and steam injection or the water injection rate of process furnace simultaneously according to inlet amount, prevent the coking of heating furnace tube overtemperature.According to the corresponding adjustment turning oil of Fractionator Bottom liquid level freshening amount, the compressor absorbing-stabilizing system is looked process furnace, the separation column operational circumstances is done corresponding the adjustment.Adjust fractionation tower top service temperature.Close top and follow the variable valve on oily thermal backflow pipeline, open gasoline cold reflux to top simultaneously and follow thermal backflow pipeline valve, regulate gasoline cold reflux flow follows oil header bottom gas phase temperature and is greater than 130 ℃ to control top simultaneously, guarantee on the one hand the quality index of gasoline and diesel oil, preventing from the other hand occurring in the oil header bottom salt crust can't process.Start dirty wash journey, the dirty medium of washing is fractionation tower top triphase separator sour water, flow process is: sour water pump, top circulating oil pump A outlet, top turning oil return tower line, top pump around circuit variable valve, fractionation tower top the first layer tower tray, sour water and top turning oil are mixed into separation column, slowly tower top temperature is controlled to below 95 ℃, guarantee that most water carries out circulation flushing in the top section of following.Sour water is flowed along tower tray from top to bottom by the separation column top, dissolve the ammonium salt on tower tray in flow process, wash away the dirt on tower tray, sewage finally enters the fractionation tower top and follows in oil header, and the pipeline that changes the separation column head space cooler of going on foot after top circulating oil pump 2 is extracted pressurization out is rinsed fractionation tower top gas pipeline and air cooler.Start the washing flow process, the washing medium is for purifying waste water, and flow process is consistent with dirty wash journey, only generally according to the separation column head temperature, adjusts gradually the flow of purifying waste water, general, the coking fractional distillation column of 1,000,000 tons of scales purify waste water flow be controlled at 30 tons/hour with interior be safe.The gasoline of separating through triphase separator follows the thermal backflow cross-line by the gasoline cold reflux to top and returns to the fractionation tower top and follow oil header bottom tower tray, desalinization of soil by flooding or leaching sewage pumps out device by fractionation tower top oily(waste)water, the online washing later stage is analyzed water sample, when analyze all ≯ 300mg/l is tested in the Cl-in draining and ammonia chlorination, stop annotating and purify waste water, wash complete.Afterwards, progressively adjust tower top temperature, recover flow process, improve treatment capacity to normal level, return to normal production.The invention effect
The operational circumstances of certain delayed coking unit separation column before and after online washing changes in Table 1.
Table 1 separation column is washed online the front and back operational condition and is changed
| Project | Before online washing | After online washing |
| The separation column pressure drop, KPa | 43.5 | 22 |
| Fractionation tower temperature, ℃ | 140 | 121 |
| Gasoline endpoint, ℃ | 220 | 182 |
| Pump follows on top | Discontinuity is found time | Operation is normal |
The accompanying drawing explanation
The online desalinization of soil by flooding or leaching process flow diagram of Fig. 1 separation column.
Wherein: 1 pipeline of purifying waste water, 2 top turning oils return the tower pipeline, 3 pipelines, 4 pipelines, 5 pipelines, 6 oil-water mixture pipelines, 7 medium gasoline pipeline, 8 gasoline cold reflux pipelines, 9 pipelines, oily thermal backflow pipeline is followed on 10 tops, hot reflux condenser spool line is followed on 11 gasoline cold refluxs to top, 12 sour water pipelines, 13 sour water pipelines, 14 raw gasline pumps, 15 triphase separators, 16 air coolers, 17 top cycle set fuel tanks, 18 separation columns, 19 top circulating oil pump A, 20 top circulating oil pump B, 21 sour water pumps,
Embodiment
As shown in the figure: after finding separation column top salt crust, at first close top and follow oily thermal backflow pipeline 10 adjusted valve A, opening gasoline cold reflux pipeline 8 follows thermal backflow pipeline connection line 11 adjusted valve B and follows oily oil header 17 bottom column plates enough liquid-phase refluxs are arranged to guarantee top to top, regulate gasoline cold reflux flow follows oil header 17 bottom gas phase temperatures and is greater than 130 ℃ to control top simultaneously, guarantee on the one hand the quality index of gasoline and diesel oil, preventing from the other hand occurring in the oil header bottom salt crust can't process; Start dirty wash journey: fractionation tower top triphase separator 15 sour waters return tower pipeline 2 by sour water pump 21, sour water pipeline 12, top turning oil and enter in separation column 18, enter top after salt on tower tray and dirt are washed and follow in oil header 17 separation column 18 is interior, by pipeline 3, variable valve C, pipeline 9, pipeline 4, extract out by walking pipeline 5 after top circulating oil pump B20 pressurization and enter separation column head space cooler 16 it is washed; Oil-water mixture after washing carries out oily water separation in oil-water mixture pipeline 6 enters fractionation tower top triphase separator 15, the gasoline of separating enters gasoline cold reflux pipeline 8 parts by medium gasoline pipeline 7, raw gasline pump 14 and returns to separation column 18, a part goes out device, and sour water advances the downstream acidic water stripping device by sour water pump 21, sour water pipeline 13; When the sour water color does not change, start the washing flow process: purify waste water and return tower pipeline 2 by top turning oil by the pipeline 1 of purifying waste water after top circulating oil pump A19 pressurization and enter in separation column 18, enter top after salt on tower tray and dirt are washed and follow in oil header 17 separation column 18 is interior, by pipeline 3, variable valve C, pipeline 9, pipeline 4, extract out by walking pipeline 5 after top circulating oil pump B20 pressurization and enter separation column head space cooler 16 it is washed; Oil-water mixture after washing carries out oily water separation in oil-water mixture pipeline 6 enters fractionation tower top triphase separator 15, the gasoline of separating enters gasoline cold reflux pipeline 8 parts by medium gasoline pipeline 7, raw gasline pump 14 and returns to separation column 18, a part goes out device, sour water advances the downstream acidic water stripping device by sour water pump 21, sour water pipeline 13, the Cl in draining
-and the ammonia chlorination stops annotating and purify waste water while testing analyze all ≯ 300mg/l, wash complete.
Claims (1)
1. the processing method of the online desalinization of soil by flooding or leaching of a delayed coking unit separation column is characterized in that:
After the salt crust of separation column top, at first close top and follow oily thermal backflow pipeline (10) adjusted valve A, open gasoline cold reflux pipeline (8) to top and follow thermal backflow pipeline connection line (11) adjusted valve B and follow oily oil header (17) bottom column plate enough liquid-phase refluxs are arranged to guarantee top, regulate gasoline cold reflux flow simultaneously and follow oil header bottom gas phase temperature and be greater than 130 ℃ to control top;
Start dirty wash journey: fractionation tower top triphase separator (15) sour water returns tower pipeline (2) by sour water pump (21), sour water pipeline (12), top turning oil and enters in separation column (18), enter top after in separation column, the salt on tower tray and dirt being washed and follow in oil header (17), by pipeline (3), variable valve C, pipeline (9), pipeline (4), extract out by walking pipeline (5) after top circulating oil pump B (20) pressurization and enter separation column head space cooler (16) it is washed; Oil-water mixture after washing carries out oily water separation in oil-water mixture pipeline (6) enters fractionation tower top triphase separator (15), the gasoline of separating enters gasoline cold reflux pipeline (8) part by medium gasoline pipeline (7), raw gasline pump (14) and returns to separation column (18), a part goes out device, and sour water advances the downstream acidic water stripping device by sour water pump (21), sour water pipeline (13);
When the sour water color does not change, start the washing flow process: purify waste water and returned tower pipeline (2) by the pipeline of purifying waste water (1) by top turning oil after top circulating oil pump A (19) pressurization and enter in separation column (18), enter top after in separation column (18), the salt on tower tray and dirt being washed and follow in oil header (17), by pipeline (3), variable valve C, pipeline (9), pipeline (4), extract out by walking pipeline (5) after top circulating oil pump B (20) pressurization and enter separation column head space cooler (16) it is washed; Oil-water mixture after washing carries out oily water separation in oil-water mixture pipeline (6) enters fractionation tower top triphase separator (15), the gasoline of separating enters gasoline cold reflux pipeline (8) part by medium gasoline pipeline (7), raw gasline pump (14) and returns to separation column (18), a part goes out device, sour water advances the downstream acidic water stripping device, the Cl in draining by sour water pump (21), sour water pipeline (13)
-and the ammonia chlorination stops annotating and purify waste water while testing analyze all ≯ 300mg/l, wash complete.
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|---|---|---|---|
| CN201110380287.1A CN103131472B (en) | 2011-11-25 | 2011-11-25 | Process method for delaying coking apparatus fractionation tower online salt washing |
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| CN201110380287.1A CN103131472B (en) | 2011-11-25 | 2011-11-25 | Process method for delaying coking apparatus fractionation tower online salt washing |
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| CN103131472B CN103131472B (en) | 2014-12-24 |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106318434A (en) * | 2015-06-16 | 2017-01-11 | 中国石油天然气股份有限公司 | Fractionation tower online salt leaching system and technology |
| CN106563285A (en) * | 2016-10-10 | 2017-04-19 | 天津科技大学 | Rectification apparatus for high-salinity material |
| CN106701193A (en) * | 2015-07-27 | 2017-05-24 | 中国石油天然气股份有限公司 | Salt-deposition-preventing open-loop on-line washing apparatus and method for top circulation system of fractionating tower |
| WO2019126429A1 (en) * | 2017-12-21 | 2019-06-27 | Uop Llc | Scale collection device for downflow reactors |
| US10537866B2 (en) | 2017-12-21 | 2020-01-21 | Uop Llc | Scale collection device for downflow reactors |
| US10549249B2 (en) | 2017-12-21 | 2020-02-04 | Uop Llc | Scale collection device for downflow reactors |
| US10576439B2 (en) | 2017-12-21 | 2020-03-03 | Uop Llc | Scale collection device for downflow reactors |
| US11224849B2 (en) | 2017-12-21 | 2022-01-18 | Uop Llc | Scale collection device for downflow reactors |
| US11298669B2 (en) | 2017-12-21 | 2022-04-12 | Uop Llc | Scale collection device for downflow reactors |
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| CN101880543A (en) * | 2010-07-02 | 2010-11-10 | 沈阳石蜡化工有限公司 | Online cleaning method of deposited salt of tower tray of normal-pressure tower |
| CN102250635A (en) * | 2010-05-21 | 2011-11-23 | 中国石油化工集团公司 | Method and device for removing salt for fractionate tower |
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2011
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102250635A (en) * | 2010-05-21 | 2011-11-23 | 中国石油化工集团公司 | Method and device for removing salt for fractionate tower |
| CN101880543A (en) * | 2010-07-02 | 2010-11-10 | 沈阳石蜡化工有限公司 | Online cleaning method of deposited salt of tower tray of normal-pressure tower |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106318434A (en) * | 2015-06-16 | 2017-01-11 | 中国石油天然气股份有限公司 | Fractionation tower online salt leaching system and technology |
| CN106318434B (en) * | 2015-06-16 | 2018-05-08 | 中国石油天然气股份有限公司 | A kind of online desalinization of soil by flooding or leaching system of fractionating column and technique |
| CN106701193A (en) * | 2015-07-27 | 2017-05-24 | 中国石油天然气股份有限公司 | Salt-deposition-preventing open-loop on-line washing apparatus and method for top circulation system of fractionating tower |
| CN106701193B (en) * | 2015-07-27 | 2019-06-07 | 中国石油天然气股份有限公司 | A kind of fractionation tower top follows the anti-salt crust of system and opens a way online water washing device and method |
| CN106563285A (en) * | 2016-10-10 | 2017-04-19 | 天津科技大学 | Rectification apparatus for high-salinity material |
| WO2019126429A1 (en) * | 2017-12-21 | 2019-06-27 | Uop Llc | Scale collection device for downflow reactors |
| US10537866B2 (en) | 2017-12-21 | 2020-01-21 | Uop Llc | Scale collection device for downflow reactors |
| US10549249B2 (en) | 2017-12-21 | 2020-02-04 | Uop Llc | Scale collection device for downflow reactors |
| US10556212B2 (en) | 2017-12-21 | 2020-02-11 | Uop Llc | Scale collection device for downflow reactors |
| US10576439B2 (en) | 2017-12-21 | 2020-03-03 | Uop Llc | Scale collection device for downflow reactors |
| US11224849B2 (en) | 2017-12-21 | 2022-01-18 | Uop Llc | Scale collection device for downflow reactors |
| US11298669B2 (en) | 2017-12-21 | 2022-04-12 | Uop Llc | Scale collection device for downflow reactors |
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| CN103131472B (en) | 2014-12-24 |
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