CN103131472B - 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
- Publication number
- CN103131472B CN103131472B CN201110380287.1A CN201110380287A CN103131472B CN 103131472 B CN103131472 B CN 103131472B CN 201110380287 A CN201110380287 A CN 201110380287A CN 103131472 B CN103131472 B CN 103131472B
- Authority
- CN
- China
- Prior art keywords
- pipeline
- oil
- water
- enters
- separation column
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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 refining of petroleum field.
Background technology
Delayed coking unit is a kind of degree of depth thermocracking process mink cell focus being converted into dry gas, liquefied gas, coker gasoline, coker gas oil, wax tailings and coke, and raw material is generally the vacuum residuum that upstream atmospheric and vacuum distillation unit comes.Because organic chloride in coking raw material and nitride can not thoroughly be removed in electric desalting process, after atmospheric and vacuum distillation unit deep drawing, this part material mainly concentrates in vacuum residuum, when vacuum residuum through process furnace be heated to 500 DEG C enter coke drum time, under the hot environment of the atoms such as N, Cl, H, O in residual oil in coke drum reaction generate N
2, NH
3, O
2deng product, in residual oil there is heat absorption hydrolysis reaction generation HCl in organic chloride and butter in coke drum simultaneously, because the oil gas generated is by NH
3be carried to rapidly in separation column with HCl, the building-up reactions in coke drum and hydrolysis reaction constantly carried out, thus produces a large amount of NH
3and HCl.In separation column, NH
3combine at suitable temperature with HCl and generate NH
4cl, NH
4cl is carried into top tower tray with minimum particle form.Tiny NH
4cl particle, on the top of separation column, is dissolved in topical hypothermia's aqueous phase, due to NH
4the boiling point of Cl solution is far above the boiling point of water, it is in decline reflux course, rising gradually due to temperature is distillated and is condensed into a kind of full-bodied semi-fluid, this semi-fluid and iron rust, coke powder etc. mix places such as being deposited on tower tray, return wire, downtake and seal pot, run up to the proper flow that to a certain degree will hinder liquid, perforate on blocking tower tray, causes separation column pressure drop to increase gradually, thus causes that separation column rushes tower, diesel oil pump is found time, gasoline endpoint is too high.As this part NH
4cl particle is fractionated overhead product when being carried to separation column head space cooler, and easily salt crust on the air cooler tube bundle of separation column top, causes separation column head space cooler cooling performance to decline, had a strong impact on the safety in production of whole device.
Summary of the invention
The object of this invention is to provide the processing method of the online desalinization of soil by flooding or leaching of a kind of delayed coking unit separation column; It is the processing method of a kind of online desalinization of soil by flooding or leaching that there is the exploitation of the problem 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 washing two processes, and can not stop work at device, do not affect quality product, outer get rid of dirty oil condition under tower tray is followed to fractionation tower top top, system is followed on top and separation column top air-cooler system is washed online, perfect existing delayed coking flow process.This safe in process environmental protection, decreases 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:
Setting device treatment capacity.The treatment capacity of the slow each branch of reduction process furnace, to zone of reasonableness, simultaneously according to the fire box temperature of inlet amount adjustment process furnace and steam injection or water injection rate, prevents the coking of heating furnace tube overtemperature.According to Fractionator Bottom liquid level corresponding adjustment turning oil freshening amount, compressor absorbing-stabilizing system looks process furnace, separation column operational circumstances does corresponding adjustment.Adjustment fractionation tower top service temperature.Close the variable valve pushing up and follow on oily thermal backflow pipeline, open gasoline cold reflux simultaneously and follow thermal backflow pipeline valve to top, regulate gasoline cold reflux flow to follow oil header bottom gas phase temperature be greater than 130 DEG C to control top simultaneously, ensure the quality index of gasoline and diesel oil on the one hand, preventing that salt crust occurs in oil header bottom on the other hand cannot process.Start dirty wash journey, 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 is mixed into separation column with top turning oil, slowly tower top temperature is controlled to less than 95 DEG C, ensure 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 separation column top, the ammonium salt on tower tray is dissolved in flow process, wash away the dirt on tower tray, sewage finally enters fractionation tower top and follows in oil header, and the pipeline changing separation column head space cooler of going on foot after pressurization extracted out by top circulating oil pump 2 rinses fractionation tower top gas pipeline and air cooler.Start washing flow process, washing medium is for purifying waste water, and flow process is consistent with dirty wash journey, only generally adjusts flow of purifying waste water gradually according to separation column head temperature, general, the flow control of purifying waste water of the coking fractional distillation column of 1,000,000 tons of scales is safe within 30 tons/hour.The gasoline separated through triphase separator to follow thermal backflow cross-line by gasoline cold reflux and returns fractionation tower top and follow oil header lower tray to top, 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 the Cl-in draining and ammonia chlorine assay all ≯ 300mg/l time, stop note to purify waste water, wash complete.Afterwards, progressively adjust tower top temperature, recover flow process, improve treatment capacity to normal level, return to normal production.Invention effect
The operational circumstances change of certain delayed coking unit separation column before and after online washing is in table 1.
The change of forward/backward operation condition washed online by table 1 separation column
| Project | Before online washing | After online washing |
| Separation column pressure drop, KPa | 43.5 | 22 |
| Fractionation tower temperature, DEG C | 140 | 121 |
| Gasoline endpoint, DEG C | 220 | 182 |
| Pump is followed on top | Discontinuity is found time | Operation is normal |
Accompanying drawing explanation
The online Salt wash process schematic flow sheet of Fig. 1 separation column.
Wherein: 1 purifies waste water pipeline, 2 top turning oils return 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, 11 gasoline cold refluxs follow hot reflux condenser spool line 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: when after the salt crust of discovery separation column top, first close top and follow variable valve A on oily thermal backflow pipeline 10, open gasoline cold reflux pipeline 8 to top to follow on thermal backflow pipeline connection line 11 variable valve B and follow oily oil header 17 lower tray have enough liquid-phase refluxs to ensure to push up, regulate gasoline cold reflux flow to follow oil header 17 bottom gas phase temperature be greater than 130 DEG C to control top simultaneously, ensure the quality index of gasoline and diesel oil on the one hand, preventing that salt crust occurs in oil header bottom on the other hand cannot process; Start dirty wash journey: fractionation tower top triphase separator 15 sour water is returned tower pipeline 2 entered in separation column 18 by sour water pump 21, sour water pipeline 12, top turning oil, entering top after washing the salt on tower tray and dirt in separation column 18 follows in oil header 17, walks pipeline 5 enter separation column head space cooler 16 and wash it by pipeline 3, variable valve C, pipeline 9, pipeline 4 after being extracted out after the circulating oil pump B20 pressurization of top; Oil-water mixture after washing enters in fractionation tower top triphase separator 15 through oil-water mixture pipeline 6 and carries out oily water separation, the gasoline separated enters gasoline cold reflux pipeline 8 part by medium gasoline pipeline 7, raw gasline pump 14 and returns separation column 18, a part goes out device, and sour water enters downstream acidic water stripping device by sour water pump 21, sour water pipeline 13; When sour water color does not change, start washing flow process: purify waste water and after top circulating oil pump A19 pressurizes, return tower pipeline 2 by top turning oil by pipeline 1 of purifying waste water and enter in separation column 18, entering top after washing the salt on tower tray and dirt in separation column 18 follows in oil header 17, walks pipeline 5 enter separation column head space cooler 16 and wash it by pipeline 3, variable valve C, pipeline 9, pipeline 4 after being extracted out after the circulating oil pump B20 pressurization of top; Oil-water mixture after washing enters in fractionation tower top triphase separator 15 through oil-water mixture pipeline 6 and carries out oily water separation, the gasoline separated enters gasoline cold reflux pipeline 8 part by medium gasoline pipeline 7, raw gasline pump 14 and returns separation column 18, a part goes out device, sour water enters downstream acidic water stripping device, as the Cl in draining by sour water pump 21, sour water pipeline 13
-and ammonia chlorine assay all ≯ 300mg/l time, stop note and purify waste water, wash complete.
Claims (1)
1. a processing method for the online desalinization of soil by flooding or leaching of delayed coking unit separation column, is characterized in that:
When after the salt crust of separation column top, first close top and follow the upper variable valve A of oily thermal backflow pipeline (10), open gasoline cold reflux pipeline (8) to top and follow the upper variable valve B of thermal backflow pipeline connection line (11) to ensure that top is followed oily oil header (17) lower tray and had enough liquid-phase refluxs, regulate gasoline cold reflux flow to follow oil header bottom gas phase temperature be greater than 130 DEG C to control top simultaneously;
Start dirty wash journey: fractionation tower top triphase separator (15) sour water is returned tower pipeline (2) entered in separation column (18) by sour water pump (21), sour water pipeline (12), top turning oil, entering top after washing the salt on tower tray and dirt in separation column follows in oil header (17), walks pipeline (5) enter separation column head space cooler (16) and wash it by pipeline A (3), variable valve C, pipeline B (9), pipeline C (4) after being extracted out after pressurizeing in top circulating oil pump B (20); Oil-water mixture after washing enters in fractionation tower top triphase separator (15) through oil-water mixture pipeline (6) and carries out oily water separation, the gasoline separated enters gasoline cold reflux pipeline (8) part by medium gasoline pipeline (7), raw gasline pump (14) and returns separation column (18), a part goes out device, and sour water enters downstream acidic water stripping device by sour water pump (21), sour water pipeline (13);
When sour water color does not change, start washing flow process: purify waste water and after pressurizeing in top circulating oil pump A (19), return tower pipeline (2) by top turning oil by pipeline of purifying waste water (1) and enter in separation column (18), entering top after washing the salt on tower tray and dirt in separation column (18) follows in oil header (17), walks pipeline (5) enter separation column head space cooler (16) and wash it by pipeline A (3), variable valve C, pipeline B (9), pipeline C (4) after being extracted out after pressurizeing in top circulating oil pump B (20); Oil-water mixture after washing enters in fractionation tower top triphase separator (15) through oil-water mixture pipeline (6) and carries out oily water separation, the gasoline separated enters gasoline cold reflux pipeline (8) part by medium gasoline pipeline (7), raw gasline pump (14) and returns separation column (18), a part goes out device, sour water enters downstream acidic water stripping device by sour water pump (21), sour water pipeline (13), when the Cl-in draining and ammonia chlorine assay all ≯ 300mg/l time, stop note to purify waste water, wash complete.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110380287.1A CN103131472B (en) | 2011-11-25 | 2011-11-25 | Process method for delaying coking apparatus fractionation tower online salt washing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110380287.1A CN103131472B (en) | 2011-11-25 | 2011-11-25 | Process method for delaying coking apparatus fractionation tower online salt washing |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103131472A CN103131472A (en) | 2013-06-05 |
| CN103131472B true CN103131472B (en) | 2014-12-24 |
Family
ID=48491932
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110380287.1A Active CN103131472B (en) | 2011-11-25 | 2011-11-25 | Process method for delaying coking apparatus fractionation tower online salt washing |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103131472B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| US10576439B2 (en) | 2017-12-21 | 2020-03-03 | Uop Llc | Scale collection device for downflow reactors |
| US10556212B2 (en) * | 2017-12-21 | 2020-02-11 | Uop Llc | Scale collection device for downflow reactors |
| US11224849B2 (en) | 2017-12-21 | 2022-01-18 | Uop Llc | Scale collection device for downflow reactors |
| US10537866B2 (en) | 2017-12-21 | 2020-01-21 | Uop Llc | Scale collection device for downflow reactors |
| US11298669B2 (en) | 2017-12-21 | 2022-04-12 | Uop Llc | Scale collection device for downflow reactors |
| US10549249B2 (en) | 2017-12-21 | 2020-02-04 | Uop Llc | Scale collection device for downflow reactors |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
-
2011
- 2011-11-25 CN CN201110380287.1A patent/CN103131472B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103131472A (en) | 2013-06-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103131472B (en) | Process method for delaying coking apparatus fractionation tower online salt washing | |
| CN108138053B (en) | Combined heat and power delayed coking device | |
| CN104419444B (en) | A kind of method utilizing the moisture sump oil of delayed coking unit freshening | |
| CN104151119B (en) | The method of octane-iso is prepared in the deep processing of a kind of carbon four | |
| CN104711008B (en) | A kind of device for preventing oil distillation column salt crust | |
| CN204151295U (en) | A kind of anti-salt crust device of liquid-liquid extraction | |
| CN104099171B (en) | A kind of continuous distillation process for waste lubricant oil regeneration | |
| CN102250635B (en) | Method and device for removing salt for fractionate tower | |
| CN103396830B (en) | Device and method for dehydrating heavy sump oil | |
| CN102703114A (en) | Method for preventing fractionating tower from salt deposition | |
| CN103194258B (en) | Method for prolonging operation period of circulation oil system on top of fractionation tower | |
| CN104178210B (en) | The method and process unit of higher boiling conduction oil are discarded in a kind of recycling | |
| CN208517188U (en) | A kind of Containing-Sulfur Wastewater Treatment System | |
| CN202337765U (en) | Refining device of swill-cooked dirty oil and used oil | |
| CN106914068A (en) | A kind of delayed coking exhaust gas treating method | |
| CN204151297U (en) | A kind of chlorion extracting corrosion-resisting device | |
| CN109666508A (en) | A kind of remodeling method promoting the hydrogenation plant economical running period | |
| CN103084004B (en) | Coke cooling water and coke cutting water mutually combined purifying and recycling method | |
| CN110642314A (en) | Process unit for comprehensively utilizing crude oil electric desalting sewage by delayed coking device | |
| CN216808705U (en) | Efficient integrated top circulating oil dechlorination system | |
| CN210462963U (en) | Dilute steam generator capable of controlling steam/hydrocarbon ratio for light hydrocarbon thermal cracking | |
| CN108893136B (en) | Treatment method of dirty oil generated by delayed coking heavy steam blowing | |
| CN203794840U (en) | Sump oil recycling device for delay coking technology | |
| CN202070192U (en) | Special oil-water separator for metal surface treatment | |
| RU2546677C1 (en) | Method and installation of hydrocracking with obtaining motor fuels |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |