CN106745442A - A kind of refinery basic sewage acidification reaction device and acidization tool - Google Patents
A kind of refinery basic sewage acidification reaction device and acidization tool Download PDFInfo
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- CN106745442A CN106745442A CN201510800824.1A CN201510800824A CN106745442A CN 106745442 A CN106745442 A CN 106745442A CN 201510800824 A CN201510800824 A CN 201510800824A CN 106745442 A CN106745442 A CN 106745442A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/26—Treatment of water, waste water, or sewage by extraction
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
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Abstract
The invention discloses a kind of refinery basic sewage acidification reaction device, including oil-gas mixer, air-fuel mixture tower, air-fuel mixture pump, acidification reaction tower and acidizing pump, oil-gas mixer import respectively with SO2Feed pipe and finish feed pipe are connected, and outlet is connected with air-fuel mixture tower import, and fiber-film contact, collecting tank, mozzle are set successively from top to bottom in air-fuel mixture tower, and mozzle bottom is deep under tower reactor liquid level；The acidification reaction tower is telescoping structure, and inner cylinder is extraction tower, and outer barrel is connected with acidification reaction tower tower reactor；Air-fuel mixture tower tower reactor is connected with acidification reaction tower tower reactor by overflow pipe, and the mixed liquor of air-fuel mixture tower tower reactor is overflowed in acidification reaction tower tower reactor by this overflow pipe.Acidization tool of the invention is realized using said apparatus.The present invention can reduce the heat that acidification reaction is produced while alkaline residue is acidified, and increase hydrogen sulfide, the absorption efficiency of mercaptan thioether that acidifying is produced；With simple structure, degree of integration is high, floor space is small, absorb and acidifying efficiency high the features such as.
Description
Technical field
The invention belongs to environment-protection wastewater processing technology field, a kind of refinery basic sewage acidification reaction device and acidization tool are related in particular to.
Background technology
In Refinery Oil alkali cleaning subtractive process, the referred to as alkaline residue of the alkaline waste liquor containing high density pollution thing can be produced, the discharge capacity of its COD, sulfide and phenol accounts for more than the 40%-50% of the such pollutant discharge amount of oil plant.These alkali residue waste liquids, if directly discharged, meeting severe contamination environment, and severe corrosion equipment.In the last few years, as national environmental protection regulation, standard are increasingly complete and strict, and people, to the cry more and more higher of improvement environmental quality, alkaline residue treatment is increasingly taken seriously.
At present, the alkaline residue processing method for commonly using predominantly neutralisation, biochemical process and wet oxidation process etc., wherein neutralisation typically carries out acidification as acidizing reagent using acidic materials such as the concentrated sulfuric acid, sulfur dioxide to alkaline residue, alkaline residue basicity, most sulfide in removal alkaline sewage are reduced, and reclaims petroleum acids, the method technique is relatively simple, plant investment is low, and water treatment effect is obvious, therefore it is a universal processing procedure to neutralize alkaline residue treatment.But, during actual alkaline residue acidification, due to containing substantial amounts of easy foaming substance in alkaline residue, and acid-base reaction releases substantial amounts of heat contributes to the generation of foam, the presence of a large amount of foams is unfavorable for radiating, hinders the carrying out of acid-base reaction, and can cause to block liquid flooding tower phenomenon, so that containing substantial amounts of alkaline residue in the tail gas of discharge, the stable operation of device is influenceed.
CN201210176565.6 discloses the combined method and device of a kind of caustic sludge desulfuration dephenolize neutralization and tail gas desulfurization treatment, wherein device includes alkaline residue oxidation sweetening tower, alkaline residue filter, carbonization settling tank, fiber film contactor and tail gas adsorption digester, alkaline residue oxidation sweetening top of tower is connected by tail gas discharging pipe one with tail gas adsorption digester, alkaline residue oxidation sweetening tower bottom is connected by alkaline residue delivery pipe with alkaline residue filter, alkaline residue filter is connected by alkaline residue feed pipe two with fiber film contactor, fiber film contactor bottom is fixed on carbonization settling tank by flange；Method is comprised the following steps：Alkaline residue is carried out the de- disulphide treatment of oxidation processes, air lift essence successively, mechanical admixture and colloid is removed, is separated hydrogen sulfide and mercaptan, absorption desulfurization process.The method alkaline residue is first had to by desulfurization process, can produce desulfidation tail gas, and is needed by that could be discharged after finish adsorption treatment, and the sulfur-bearing finish after absorption tail gas goes finished pot to reconcile.Alkaline residue after desulfurization process needs to add 1-5 times of fresh water or demineralized water to dilute, and can just carry out neutralisation treatment.
CN200920199634.9 and US5997731 disclose the alkaline residue handling process of a kind of sulfur-bearing and phenol, neutralized using fiber-film contact combination carbon dioxide and gasoline extracting dephenolize technology, its advantage is that the carbonization treatments such as phenol sodium are generated into phenol and niter cake, vulcanized sodium carbonization treatment is generated into hydrogen sulfide and sodium carbonate, by the small organic molecule separate out such as mercaptan thioether, in can the hydrogen sulfide that generated, phenol and mercaptan thioether extract back into light-end products, the process problem of generation hydrogen sulfide, phenol and mercaptan thioether in carbonisation is solved.But to be acidified using carbon dioxide that necessarily cause alkaline residue acidifying not thorough in the technique, so that the clearance of the pollutant such as alkaline residue COD is poor, and it is high using the device integrated level of this technique, carbon dioxide is poor with the blended absorbent efficiency of oil product, so that inefficient and installation area the increase of acidifying, what is more important, due to producing substantial amounts of neutralization reaction heat in acidization, substantially reduces extraction efficiency.
The content of the invention
In view of the shortcomings of the prior art, it is an object of the invention to provide a kind of refinery basic sewage acidification reaction device and acidization tool.The present invention can reduce the heat that acidification reaction is produced while alkaline residue is acidified, and greatly increase hydrogen sulfide, the absorption efficiency of mercaptan thioether that acidifying is produced；And acidification reaction device has that simple structure, degree of integration are high, floor space is small, absorb and the features such as acidifying efficiency high.
Refinery basic sewage acidification reaction device of the present invention, including oil-gas mixer, air-fuel mixture tower, air-fuel mixture pump, acidification reaction tower and acidizing pump, wherein oil-gas mixer import respectively with SO2Gas feed pipe and finish feed pipe are connected, and outlet is connected with air-fuel mixture tower import, and fiber-film contact, collecting tank, mozzle are set successively from top to bottom in air-fuel mixture tower, and mozzle bottom is deep under tower reactor liquid level；Air-fuel mixture pump inlet is connected with air-fuel mixture tower tower reactor, and outlet is connected with finish feed pipe；The acidification reaction tower is telescoping structure, and inner cylinder is extraction tower, and outer barrel is connected with acidification reaction tower tower reactor；Acidifying pump inlet is connected with acidification reaction tower tower reactor, and outlet is connected with extraction tower bottom；Air-fuel mixture tower tower reactor is connected with acidification reaction tower tower reactor by overflow pipe, and the mixed liquor of air-fuel mixture tower tower reactor is overflowed in acidification reaction tower tower reactor by this overflow pipe.
The oil-gas mixer uses air-fuel mixture pump or pipe-line mixer, it is possible to achieve SO2The premixing of gas and finish.Oil-gas mixer preferably uses multiphase flow pump, can not only realize SO2Gas and finish are sufficiently mixed, and can improve finish to SO2Absorbability, be favorably improved acidizing effect.
The air-fuel mixture tower uses conventional use of cylindricality tower with acidification reaction tower, and ratio of height to diameter is 8-20, preferably 10-18；Tower reactor diameter is 1-5 with upper end tower body diameter ratio, and preferably tower reactor is with diameter greater than upper end tower body diameter.The collecting tank is preferably disposed in air-fuel mixture tower tower reactor, and collecting tank lower end is uniformly arranged multiple a diameter of 10-40mm mozzles, and mozzle bottom is deep under tower reactor liquid level.The mozzle for setting in principle is The more the better, can make mixed effect more preferably.
The acidification reaction tower outer barrel diameter is 1.1-2 times of inner cylinder extraction tower diameter, and outer barrel upper end open is communicated with air, and lower end connects with tower reactor.The upper end sealing of the inner cylinder extraction tower, the cylindricality tower using upper-end inner diameter more than bottom diameter, it is preferred to use upper end sets tapered reaction tower, the conical surface of upper end taper tower wall is provided with downwards multiple extractant overfalls, and the quantity of overfall is The more the better in principle.The extraction tower does not limit specific form, can be the extraction tower form of the transmissions such as spray column, perforated-plate extraction tower, packed extraction tower and turntable extracting tower.
Another object of the present invention is also resided in and provides a kind of acidization tool using above-mentioned refinery basic sewage acidification reaction device, including following content：
（1）Finish and SO2Gas is pre-mixed in being passed through oil-gas mixer, then pass to carry out double absorption in the fiber-film contact in air-fuel mixture tower, to finally enter entered into by mozzle in collecting tank and depth absorption is carried out under tower reactor liquid level, and blended absorbent repeatedly is carried out by air-fuel mixture pump；
（2）Absorb SO2Finish afterwards, in being overflowed to acidification reaction tower tower reactor by overflow pipe from air-fuel mixture tower tower reactor, and is sent to extraction tower and carries out adverse current acidizing extraction reaction with refinery basic sewage by acidizing pump；
（3）The bubble that the rich absorbent oil agent of extractive reaction and acidifying are produced is flowed down, while not being discharged to outside tower by the passage between inner cylinder and outer barrel by the gas that finish absorbs along acidification reaction tower outer tube inner wall by being arranged on several overfalls of extraction tower upper end from above；
（4）Alkaline residue is discharged to outside system in extraction tower bottom after acidifying, while rich absorbent oil agent is discharged to outside system by acidizing pump.
In the present invention, step（1）SO can directly be used2Purified gases, it would however also be possible to employ contain SO2Gas, such as use S-Zorb adsorbent reactivation flue gases, be passed through a certain amount of inert gas such as nitrogen and blended, control SO2Volumetric concentration is 5%-80%.The finish is the finish that kerosene raffinate to be hydrogenated with, diesel oil, naphtha etc. prepare into hydrogenation device for treatment, the finish and SO2It is 0.005-0.5, preferably 0.02-0.1 with the volume ratio of inert gas gaseous mixture；The operating pressure of mixed process is controlled to be less than 10kPa.SO of the present invention2It is pre-mixed in oil-gas mixer first with finish with inert gas gaseous mixture, then pass to carry out secondary blended absorbent in the fiber-film contact in air-fuel mixture tower, to finally enter entered into below tower reactor finish liquid level by mozzle in the collecting tank of air-fuel mixture tower lower end and carry out depth blended absorbent, operated by above-mentioned blended absorbent, finish has been significantly greatly increased to SO2Absorption efficiency.
In the present invention, step（2）Absorb SO2There is neutralization reaction with alkali residue waste liquid in finish afterwards, with the carrying out of acidification reaction, most of organic sulfur compound, H in alkali residue waste liquid2S, phenol etc. are entered in finish with molecular conformation.During acidification, control operation pressure is less than 10kPa；The ratio of alkaline residue and finish is 1:1-1:30, preferably 1:3-1:10, to ensure the thorough removal of sulfide and petroleum acids, finally give the acidifying solution that pH is 2-5.After acidified treatment, the COD clearances of alkali residue waste liquid up to more than 90%, organic sulfur compound and H2Up to more than 99%, volatile phenol clearance is up to more than 95% for S clearances.
In the present invention, step（3）Big calorimetric is released in the acidization, temperature is raised and is unfavorable for organic sulfur compound, H that finish is produced to acidization2The absorption of the pollutants such as S, phenol, therefore the present invention uses following methods to discharge heat, reduces and absorbs finish temperature：Several overfall overflows of rich absorbent oil agent after extraction by being arranged on extraction tower upper end are got off, and preferably setting mozzle in overfall flows down rich absorbent oil agent along acidification reaction tower outer tube inner wall wall, due to inert gas, such as N2Solubility in finish is far smaller than SO2, therefore inert gas is discharged to outside acidification reaction tower by the passage between inner cylinder and outer barrel from the bottom to top, the inert gas finish higher with the temperature got off from upper end overflow is inversely contacted, and makes the reduction of finish temperature, so as to increase the absorption efficiency of finish.The inert gas of discharge can enter incinerator, or part returns to oil-gas mixer and re-starts air-fuel mixture.
In the present invention, step（4）Rich absorbent oil agent after the partial extraction absorption enters hydro-refining unit and is processed.
Compared with prior art, the present invention has following features：
（1）The present invention does not need pre-desulfurization, and acidization does not produce acidifying tail gas, non-secondary pollution, and acidizing device simple structure, degree of integration are high, floor space is small.
（2）SO2Depth blended absorbent with finish successively carries out oil-gas mixer premixing, two grades of blended absorbents of fiber-film contact and collecting tank and mozzle, considerably increases finish to SO2Absorption efficiency.
（3））With CO2Compared as acidizing reagent, using SO2With inert gas gaseous mixture as acidizing reagent, deepen alkaline residue acidifying depth, souring operation condition is just reached pollutants removal rate higher at ambient pressure, greatly reduce plant construction cost and operation difficulty.And due to inert gas and SO2Different solubility in finish, the inert gas discharged in acidization is inversely contacted with the high temperature finish produced in acidization, and high degree reduces finish temperature, so as to improve absorption finish to organic sulfur compound, H2The absorption efficiency of the pollutants such as S, phenol.
（4）Because present apparatus acidification reaction tower upper end sets overfall, make to produce a large amount of bubbles to overflow back tower reactor in refinery basic sewage acidization, so as to effectively prevent the phenomenons such as liquid foam entrainment.
Brief description of the drawings
Fig. 1 is a kind of structural representation of acidification reaction device of the present invention；
Description of symbols in figure：1-SO2With inert gas gaseous mixture, 2- finishes, 3- oil-gas mixers, 4- air-fuel mixture pumps, 5- air-fuel mixture towers, 6- fiber-film contacts, 7- collecting tanks, 8- collecting tank mozzles, 9- air-fuel mixture tower tower reactors, 10- overflow pipes, 11- acidification reaction tower tower reactors, 12- acidification reaction towers, 13- extraction towers, 14- extraction tower packings, 15- extraction tower overfalls, 16- inert gases, 17- refinery basic sewages, 18- acidizing pumps, alkaline residue, 20- rich absorbent oil agent, 21- acidification reaction tower outer barrels after 19- acidifyings.
Specific embodiment
Refinery basic sewage acidification reaction device of the present invention as shown in Figure 1, including oil-gas mixer 3, air-fuel mixture tower 5, air-fuel mixture pump 4, acidification reaction tower 12 and acidizing pump 18.The import of oil-gas mixer 3 respectively with SO2Connected with the feed pipe of inert gas gaseous mixture 1 and the feed pipe of finish 2, oil-gas mixer outlet is connected with the import of air-fuel mixture tower 5.Fiber-film contact 6, collecting tank 7, mozzle 8 are set successively from top to bottom in air-fuel mixture tower, the bottom of mozzle 8 is deep under the liquid level of air-fuel mixture tower tower reactor 9.The import of air-fuel mixture pump 4 is connected with air-fuel mixture tower tower reactor 9, and outlet is connected with the feed pipe of finish 2；The acidification reaction tower 12 is telescoping structure, and inner cylinder is extraction tower 13, and outer barrel 21 is connected with acidification reaction tower tower reactor 11；The import of acidizing pump 18 is connected with acidification reaction tower tower reactor 11, and outlet is connected with extraction tower bottom；Air-fuel mixture tower tower reactor is connected with acidification reaction tower tower reactor by overflow pipe 10, and the mixed liquor of air-fuel mixture tower tower reactor is overflowed in acidification reaction tower tower reactor by this overflow pipe.
The oil-gas mixer uses pipe-line mixer or multiphase flow pump.The air-fuel mixture tower uses conventional use of cylindricality tower with acidification reaction tower, and ratio of height to diameter is 8-20, preferably 10-18；Tower reactor diameter is 1-5, preferably greater than upper end tower body diameter with upper end tower body diameter ratio.The collecting tank is located in air-fuel mixture tower tower reactor, and collecting tank lower end is uniformly arranged multiple a diameter of 10-40mm mozzles, and mozzle bottom needs to be deep under tower reactor liquid level.The mozzle for setting in principle is The more the better.
The acidification reaction tower outer barrel diameter is 1.1-2 times of inner cylinder extraction tower diameter, and outer barrel upper end open is communicated with air, and lower end connects with tower reactor.The upper end sealing of the inner cylinder extraction tower, tapered reaction tower is set using upper end, and the conical surface of upper end taper tower wall is provided with downwards multiple extractant overfalls 15, and the quantity of overfall is The more the better in principle.The extraction tower is provided with filler 14.
When above-mentioned acidification reaction device works, SO first2It is passed through in oil-gas mixer 3 simultaneously with finish 2 with inert gas gaseous mixture 1 and is tentatively mixed, secondary blended absorbent is carried out subsequently into the fiber-film contact 6 in air-fuel mixture tower 5, to finally enter entered into by mozzle 8 in collecting tank 7 and depth blended absorbent is carried out under tower reactor liquid level, and blended absorbent repeatedly is carried out by air-fuel mixture pump 4.Absorb SO2Finish afterwards, in overflowing to acidification reaction tower tower reactor 11 by overflow pipe 10 from air-fuel mixture tower tower reactor 9, and is sent to extract the refinery basic sewage 17 that the lower end of tower packing 14 feeds with extraction tower packing upper end and carries out adverse current acidizing extraction reaction by acidizing pump 18.Rich absorbent oil agent 20 that extractive reaction is produced and the bubble that is produced in acidization are by being arranged on several overfalls 15 of extraction tower upper end, flowed down from above along the inwall of acidification reaction tower tower body outer barrel 21, while not being discharged to outside acidification reaction tower 12 by the passage between inner cylinder and outer barrel from the bottom to top by the inert gas 16 that finish absorbs；Alkaline residue 19 is discharged to outside system in the bottom of extraction tower 13 after acidifying, while rich absorbent oil agent 20 is also discharged to outside system by acidizing pump 18.
Technical scheme and effect are described in detail with reference to embodiment.
Embodiment 1
Certain plant catalytic gasoline alkaline residue, wherein COD is 3.21 × 105Mg/L, sulfide is 1.76 × 104mg/L.Acidification is carried out to it using the acidification reaction device of accompanying drawing 1, oil-gas mixer uses pipe-line mixer, and air-fuel mixture tower is 10 with the ratio of height to diameter of acidification reaction tower, air-fuel mixture tower tower reactor is 2 with upper end tower body diameter ratio with acidification reaction tower tower reactor diameter.Collecting tank in air-fuel mixture tower tower reactor is opened type cube structure, is arranged in tower reactor, and collecting tank lower end is uniformly arranged 30 mozzles of a diameter of 15mm.Acidification reaction tower outer barrel diameter is 1.2 times of inner cylinder extraction tower diameter, and upper end open is communicated with air, and lower end connects with acidification reaction tower tower reactor.Extraction tower is packed tower, and upper end sets tapered, and the conical surface of taper tower wall is provided with 8 extractant overfalls downwards.Using from S-Zorb adsorbent reactivation flue gases, it is passed through nitrogen and is blended, controls SO2Volumetric concentration is 5%, and the finish for using is to treat hydrofining diesel oil, finish and SO2It is 0.05 with the volume ratio of the gaseous mixture of inert gas；The operating pressure of mixed process is less than 10kPa.When alkaline residue is acidified, the ratio of alkaline residue and finish is 1:4, finally give the acidifying solution that pH is 5 or so.After acidified treatment, the COD clearances of alkali residue waste liquid are 90%, organic sulfur compound and H2Up to 99%, volatile phenol clearance is up to 95% for S clearances.
Embodiment 2
Certain plant catalytic gasoline alkaline residue, wherein COD is 7.97 × 104Mg/L, sulfide is 4 × 103mg/L.Acidification is carried out to it using the acidification reaction device of accompanying drawing 1, oil-gas mixer uses pipe-line mixer, and air-fuel mixture tower is 18 with the ratio of height to diameter of acidification reaction tower, air-fuel mixture tower tower reactor is 5 with upper end tower body diameter ratio with acidification reaction tower tower reactor diameter.Collecting tank in air-fuel mixture tower tower reactor is hemisphere, and cambered surface down, is arranged in tower reactor, and collecting tank lower end is uniformly arranged 20 mozzles of a diameter of 40mm.Acidification reaction tower outer barrel diameter is 2 times of inner cylinder extraction tower diameter, and upper end open is communicated with air, and lower end connects with acidification reaction tower tower reactor.Extraction tower is packed tower, and upper end sets tapered, and the conical surface of taper tower wall is provided with 4 extractant overfalls downwards.Using pure SO2Gas, is passed through nitrogen and is blended, and controls SO2Volumetric concentration is 10%, and the finish for using is to treat hydrofinishing naphtha, finish and SO2It is 0.5 with the volume ratio of the gaseous mixture of inert gas；The operating pressure of mixed process is less than 10kPa.When alkaline residue is acidified, the ratio of alkaline residue and finish is 1:10, finally give the acidifying solution that pH is 4 or so.After acidified treatment, the COD clearances of alkali residue waste liquid are 94%, organic sulfur compound and H2Up to 99%, volatile phenol clearance is up to 96% for S clearances.
Embodiment 3
With operating condition with embodiment 1, difference is handling process：Pipe-line mixer is replaced using multiphase flow pump, due to improve finish to SO2Absorbability, finally give the acidifying solution that pH is 4 or so.After acidified treatment, the COD clearances of alkali residue waste liquid are 93%, organic sulfur compound and H2Up to 99%, volatile phenol clearance is up to 97% for S clearances.
Embodiment 4
With operating condition with embodiment 2, difference is handling process：Pipe-line mixer is replaced using multiphase flow pump, due to improve finish to SO2Absorbability, finally give the acidifying solution that pH is 3 or so.After acidified treatment, the COD clearances of alkali residue waste liquid are 95%, organic sulfur compound and H2Up to 99%, volatile phenol clearance is up to 98% for S clearances.
Comparative example 1
With operating condition with embodiment 1, difference is handling process：Collecting tank and mozzle are not provided with air-fuel mixture tower tower reactor, the acidifying solution that pH is 6 or so is finally given.After acidified treatment, the COD clearances of alkali residue waste liquid are 86%, organic sulfur compound and H2S clearances are 98%, and volatile phenol clearance is 93%, and removal effect declines.
Comparative example 2
With operating condition with embodiment 1, difference is handling process：Acidification reaction does not use inner/outer drum structure and overflow pipe, using common spray column.After acidified treatment, the COD clearances of alkali residue waste liquid are 71%, organic sulfur compound and H2S clearances are 98%, and volatile phenol clearance is 65%.
Comparative example 3
With operating condition with embodiment 1, difference is handling process：Inert gas is not passed through, but is passed through air and is blended.Due to introducing oxygen in system so that contain substantial amounts of sulfate radical after acidifying in alkaline residue, it is not suitable for being processed using causticization regeneration technology；And there is flammability hazard when mixing with gasoline in gas, reduce the applicability of device.
Claims (13)
1. a kind of refinery basic sewage acidification reaction device, it is characterised in that including oil-gas mixer, air-fuel mixture tower, air-fuel mixture pump, acidification reaction tower and acidizing pump, wherein oil-gas mixer import respectively with SO2Gas feed pipe and finish feed pipe are connected, and outlet is connected with air-fuel mixture tower import, and fiber-film contact, collecting tank, mozzle are set successively from top to bottom in air-fuel mixture tower, and mozzle bottom is deep under tower reactor liquid level；Air-fuel mixture pump inlet is connected with air-fuel mixture tower tower reactor, and outlet is connected with finish feed pipe；The acidification reaction tower is telescoping structure, and inner cylinder is extraction tower, and outer barrel is connected with acidification reaction tower tower reactor；Acidifying pump inlet is connected with acidification reaction tower tower reactor, and outlet is connected with extraction tower bottom；Air-fuel mixture tower tower reactor is connected with acidification reaction tower tower reactor by overflow pipe, and the mixed liquor of air-fuel mixture tower tower reactor is overflowed in acidification reaction tower tower reactor by this overflow pipe.
2. device according to claim 1, it is characterised in that：The oil-gas mixer uses multiphase flow pump.
3. device according to claim 1, it is characterised in that：The air-fuel mixture tower uses cylindricality tower with acidification reaction tower, and ratio of height to diameter is 8-20, and tower reactor diameter is 1-5 with upper end tower body diameter ratio.
4. device according to claim 1, it is characterised in that：The collecting tank is arranged in air-fuel mixture tower tower reactor, and collecting tank lower end is uniformly arranged multiple a diameter of 10-40mm mozzles, and mozzle bottom is deep under tower reactor liquid level.
5. device according to claim 1, it is characterised in that：The acidification reaction tower outer barrel diameter is 1.1-2 times of inner cylinder extraction tower diameter, and outer barrel upper end open is communicated with air, and lower end connects with tower reactor.
6. device according to claim 1, it is characterised in that：The inner cylinder extraction tower is the extraction tower form of the transmissions such as spray column, perforated-plate extraction tower, packed extraction tower and turntable extracting tower, and upper end sealing sets tapered reaction tower using upper end, and the conical surface of upper end taper tower wall is provided with downwards multiple extractant overfalls.
7. using the refinery basic sewage acidization tool of the claim any described devices of 1-6, it is characterised in that including following content：
（1）Finish and SO2Gas is pre-mixed in being passed through oil-gas mixer, then pass to carry out double absorption in the fiber-film contact in air-fuel mixture tower, to finally enter entered into by mozzle in collecting tank and depth absorption is carried out under tower reactor liquid level, and blended absorbent repeatedly is carried out by air-fuel mixture pump；
（2）Absorb SO2Finish afterwards, in being overflowed to acidification reaction tower tower reactor by overflow pipe from air-fuel mixture tower tower reactor, and is sent to extraction tower and carries out adverse current acidizing extraction reaction with refinery basic sewage by acidizing pump；
（3）The bubble that the rich absorbent oil agent of extractive reaction and acidifying are produced is flowed down, while not being discharged to outside tower by the passage between inner cylinder and outer barrel by the gas that finish absorbs along acidification reaction tower outer tube inner wall by being arranged on several overfalls of extraction tower upper end from above；
（4）Alkaline residue is discharged to outside system in extraction tower bottom after acidifying, while rich absorbent oil agent is discharged to outside system by acidizing pump.
8. method according to claim 7, it is characterised in that：Step（1）Using pure SO2Gas contains SO2Gas, be passed through a certain amount of inert gas such as nitrogen and blended, control SO2Volumetric concentration is 5%-80%.
9. method according to claim 8, it is characterised in that：Step（1）Using S-Zorb adsorbent reactivation flue gases, it is passed through nitrogen and is blended.
10. method according to claim 7, it is characterised in that：The finish is the finish that kerosene raffinate to be hydrogenated with, diesel oil or naphtha etc. prepare into hydrogenation device for treatment, the finish and SO2It is 0.005-0.5, preferably 0.02-0.1 with the volume ratio of inert gas gaseous mixture；The operating pressure of mixed process is controlled to be less than 10kPa.
11. methods according to claim 7, it is characterised in that：Step（2）During acidification, control operation pressure is less than 10kPa；The ratio of alkaline residue and finish is 1:1-1:30, preferably 1:3-1:10, to ensure the thorough removal of sulfide and petroleum acids, finally give the acidifying solution that pH is 2-5.
12. methods according to claim 7, it is characterised in that：Step（3）Several overfall overflows of rich absorbent oil agent after extraction by being arranged on extraction tower upper end are got off, and setting mozzle in overfall flows down rich absorbent oil agent along acidification reaction tower outer tube inner wall wall.
13. methods according to claim 7, it is characterised in that：Step（4）Rich absorbent oil agent after the extraction absorption enters hydro-refining unit and is processed.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109095584A (en) * | 2018-09-25 | 2018-12-28 | 孙勇 | A kind of refinery alkaline residue treatment process |
| CN109095583A (en) * | 2018-09-25 | 2018-12-28 | 孙勇 | A kind of Integrated Processing Unit of refinery alkaline residue |
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| CN1330968A (en) * | 2000-06-28 | 2002-01-16 | 中国石油化工集团公司 | Process for comprehensive treatment of acid and alkali dregs |
| CN201579249U (en) * | 2009-11-05 | 2010-09-15 | 宁波中一石化科技有限公司 | Device for treating alkaline residue generated by desulfurizing light oil |
| CN102442738A (en) * | 2010-10-14 | 2012-05-09 | 刘宽 | Treatment process of alkaline residue during sweetening of light hydrocarbon |
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| CN109095584A (en) * | 2018-09-25 | 2018-12-28 | 孙勇 | A kind of refinery alkaline residue treatment process |
| CN109095583A (en) * | 2018-09-25 | 2018-12-28 | 孙勇 | A kind of Integrated Processing Unit of refinery alkaline residue |
| CN109095583B (en) * | 2018-09-25 | 2021-10-29 | 东营联合石化有限责任公司 | Comprehensive treatment device for oil refining alkaline residue waste liquid |
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| CN106745442B (en) | 2019-09-10 |
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