CN204385135U - Full cut catalytic gasoline selective hydrodesulfurization device - Google Patents
Full cut catalytic gasoline selective hydrodesulfurization device Download PDFInfo
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- CN204385135U CN204385135U CN201420869127.2U CN201420869127U CN204385135U CN 204385135 U CN204385135 U CN 204385135U CN 201420869127 U CN201420869127 U CN 201420869127U CN 204385135 U CN204385135 U CN 204385135U
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Abstract
The utility model relates to a kind of full cut catalytic gasoline selective hydrodesulfurization device, it is characterized in that comprising: strainer, stock oil surge tank, multiple interchanger, multiple condenser, dialkene removal reactor, hydrodesulphurisatioreactors reactors, hydro-sweetening reactor, process furnace, condenser and stripping tower etc.Compared with prior art, the utility model adopts three reactors in series operations, gasoline is without fractionation, direct hydrogenation desulfurization, compared with similar technique, gasoline product quality reaches state five standard, loss of octane number ≯ 0.7, and flow process is short, it is low to invest, process cost is economized, and energy conservation and consumption reduction effects is given prominence to, and has broad application prospects.
Description
Technical field
The utility model relates to chemical plant installations and technique, specifically refers to a kind of full cut catalytic gasoline selective hydrodesulfurization device.
Background technology
Catalytic gasoline has low-sulfur and high-octane feature, and be one of main blend component of China's gasoline, sulphur content is 200 ~ 600mg/kg about, when producing country's three gasoline, generally can meet specification of quality after being in harmonious proportion with other low-sulfur component.But under the overall background that gasoline product quality is constantly upgraded, after particularly gasoline starts state of enforcement four, state five standard, it is imperative that catalytic gasoline carries out desulfurization.
Current catalyzed gasoline hydrogenation desulfurization technique adopts the independent hydrogenation technique of heavy petrol substantially.Gasoline is through prefractionation, and cut into light, heavy petrol, heavy petrol is mixed into final treated gasoline product again through hydrogenating desulfurization with petroleum naphtha.There is the shortcoming that loss of octane number is comparatively large, reactor pressure decrease rises soon, the operational cycle is short in prior art, and needs to carry out caustic wash desulfuration alcohol or alkali-free sweetening, long flow path to raw material, invests high.
Summary of the invention
Technical problem to be solved in the utility model provides for the present situation of prior art the full cut catalytic gasoline selective hydrodesulfurization device that a kind of desulfuration selectivity is good, loss of octane number is little, reduced investment, energy consumption are low.
The utility model solves the problems of the technologies described above adopted technical scheme: this full cut catalytic gasoline selective hydrodesulfurization device, is characterized in that comprising:
The strainer be connected successively with stock oil pipeline and stock oil surge tank, the outlet at bottom of stock oil surge tank connects the first channel entrance of First Heat Exchanger by the first pump, first channel outlet connection first connecting tube of described First Heat Exchanger, be connected the first channel of the second interchanger after described first connecting tube is connected with the first Hydrogen Line again, the first channel of the second interchanger connects the material inlet of dialkene removal reactor;
The material outlet connection outlet pipeline of described dialkene removal reactor, outlet conduit connects the first channel of the 3rd interchanger, and the first channel outlet of described 3rd interchanger connects the material inlet of hydrodesulphurisatioreactors reactors;
The material outlet of described hydrodesulphurisatioreactors reactors connects the material inlet of hydro-sweetening reactor by the first channel of process furnace, the material outlet of described hydro-sweetening reactor connects the second passage of described 3rd interchanger, the second passage of described second interchanger, the second passage of the 4th interchanger and the first condenser successively, then connects the material inlet of product separation device;
The gaseous phase outlet of described product separation device connects cyclone separator by the second condenser, the outlet of described cyclone separator connects the material inlet of circulation desulfurization tower, the material outlet of described circulation desulfurization tower connects new hydrogen pipeline by the 4th Hydrogen Line, then enters gas-liquid separator together;
The gaseous phase outlet of described gas-liquid separator connects compressor, and the outlet of compressor connects described first Hydrogen Line, the second Hydrogen Line and the 3rd Hydrogen Line respectively; Described 3rd Hydrogen Line connects the outlet conduit of described dialkene removal reactor by the second passage of described process furnace; Described second Hydrogen Line connects the intermediate raw material entrance of described dialkene removal reactor;
The oil phase outlet of described product separation device connects the second passage of described 4th interchanger by second pipe, then enter the material inlet of stripping tower; The oil phase outlet of described product separation device also connects the 3rd pipeline simultaneously, and the 3rd pipeline connects the intermediate raw material entrance of described hydrodesulphurisatioreactors reactors by the 4th pump;
The tower top outlet of described stripping tower connects return tank, the gaseous phase outlet of described return tank connects the absorbing-stabilizing system of catalytic cracking unit, the liquid-phase outlet of described return tank returns described stripping tower by the 3rd pump, and the sewage outlet of described return tank connects downstream wastewater treatment unit; The bottom of described stripping tower is provided with reboiler, and the heat source passages of described reboiler connects low-pressure steam transport pipe.
As improvement, the inherent top of tower tray of tower body of described circulation desulfurization tower and the below of absorption liquid entrance are provided with fluid-tight dish, and fluid-tight dish is provided with the breach for entering for checking maintenance personnel; The upper cover position of tower body is also provided with the tube sheet for installing cyclone pipe, and described tube sheet and cyclone pipe are for removably connecting; Position corresponding to breach is provided with manhole on tower body; Described cyclone pipe has many, and the upper end of cyclone pipe is connected on tube sheet, and the upper port of cyclone pipe is stretched out tube sheet and exposed; The lower port of cyclone pipe is positioned at the top of described fluid-tight dish; Described fluid-tight dish is also provided with the thrust-augmenting nozzle for being imported to by the hydrops above fluid-tight dish on the seal pot of column plate, the outlet of described thrust-augmenting nozzle is positioned at the below of fluid-tight dish and the seal pot of subtend column plate; The entrance of thrust-augmenting nozzle is positioned at the top of fluid-tight dish, and the entrance of thrust-augmenting nozzle is higher than the outlet of described cyclone pipe.
Compared with prior art, the utility model adopts the operation of three reactors in series, gasoline without fractionation, direct hydrogenation desulfurization, flow process is short, it is low to invest, process cost is economized, and energy conservation and consumption reduction effects is given prominence to; Quality of gasoline reaches state five standard compared with similar technique, and after guarantee gasoline hydrodesulfurizationmethod while sulphur content ≯ 10mg/kg index, gasoline octane rating loss can be made to reach low-down level, and △ RON ≯ 0.7 unit, has broad application prospects.
Accompanying drawing explanation
Fig. 1 is the utility model embodiment schematic diagram;
Fig. 2 is the cross-sectional schematic on circulation desulfurization tower top in the utility model embodiment;
Fig. 3 is the sectional view along A-A line in Fig. 2;
Fig. 4 is the sectional view along B-B line in Fig. 2.
Embodiment
Below in conjunction with accompanying drawing embodiment, the utility model is described in further detail.
First the structure of the circulation desulfurization tower used in lower the present embodiment is introduced.
As shown in Figures 1 to 4, circulation desulfurization tower 7 comprises:
Tower body 71, is provided with column plate 712 in tower body 71, the top of tower body 71 is provided with gaseous phase outlet 711.In tower body and tower tower plate structure can select as required of the prior art any one.The technical scheme of the present embodiment can directly apply to the transformation of existing circulation desulfurization tower.The top of tower body is provided with absorption liquid entrance 714.
Fluid-tight dish 72, is fixed in tower body, to be positioned at above column plate and below absorption liquid entrance.Fluid-tight dish 72 is provided with breach 721, for entering in tower body 71 from this breach for checking maintenance personnel.
Tube sheet 73, is arranged on tower body upper cover position, for installing cyclone pipe 75.Tube sheet and cyclone pipe 75 are for removably connecting, and the present embodiment is for being threaded.
Manhole 74, is arranged on tower body 71 corresponding to breach 721, for from then on entering in tower body 71 for checking maintenance personnel.
Cyclone pipe 75, has many, and its upper end is connected on tube sheet 73, and the upper port of cyclone pipe 75 is stretched out tube sheet 73 and exposed; The lower port of cyclone pipe is positioned at the top of fluid-tight dish 72.
Thrust-augmenting nozzle 76, is fixed on fluid-tight dish 72, for the hydrops above fluid-tight dish 72 being imported to the seal pot 713 of column plate.The outlet of thrust-augmenting nozzle 76 is positioned at the below of fluid-tight dish 72 and the seal pot 713 of subtend column plate; The entrance of thrust-augmenting nozzle 76 is positioned at the top of fluid-tight dish 72, and the entrance of thrust-augmenting nozzle 76 is positioned at the outlet position higher than cyclone pipe 75.The height that thrust-augmenting nozzle 76 exceeds fluid-tight dish 72 is height liquid seal.
Full cut catalytic gasoline selective hydrodesulfurization device in the present embodiment comprises:
The strainer 13 be connected successively with stock oil pipeline and stock oil surge tank 9, the top of stock oil surge tank connects nitrogen pipeline, the outlet at bottom of stock oil surge tank connects the first channel entrance of First Heat Exchanger 51 by the first pump 84, first channel outlet connection first connecting tube 81 of described First Heat Exchanger 51, be connected the first channel of the second interchanger 52 after described first connecting tube 81 is connected with the first Hydrogen Line 91 again, the first channel of the second interchanger 52 connects the material inlet of dialkene removal reactor;
The material outlet connection outlet pipeline of described dialkene removal reactor, outlet conduit connects the first channel of the 3rd interchanger 53, and the first channel outlet of described 3rd interchanger 53 connects the material inlet of hydrodesulphurisatioreactors reactors 2;
The material outlet of described hydrodesulphurisatioreactors reactors connects the material inlet of hydro-sweetening reactor by the first channel of process furnace 3, the material outlet of described hydro-sweetening reactor connects the second passage of described 3rd interchanger 53, the second passage of described second interchanger 52, the second passage of the 4th interchanger 54 and the first condenser 61 successively, then connects the material inlet of product separation device 10;
The gaseous phase outlet of described product separation device 10 connects cyclone separator 8 by condenser, the outlet of described cyclone separator 8 connects the material inlet of circulation desulfurization tower 7, the material outlet of described circulation desulfurization tower 7 connects new hydrogen pipeline 95 by the 4th Hydrogen Line 94, then enters gas-liquid separator 6 together;
The gaseous phase outlet of described gas-liquid separator 6 connects compressor 5, and the outlet of compressor 5 connects described first Hydrogen Line 91, second Hydrogen Line 92 and the 3rd Hydrogen Line 93 respectively; Described 3rd Hydrogen Line 93 connects the outlet conduit of described dialkene removal reactor 1 by the second passage of described process furnace 3; Described second Hydrogen Line 92 connects the intermediate raw material entrance of described dialkene removal reactor;
The oil phase outlet of described product separation device 10 connects the second passage of described 4th interchanger 54 by second pipe 82, then enter the material inlet of stripping tower 11; The oil phase of described product separation device 10 exports the intermediate raw material entrance also connecting the 3rd pipeline the 83, three pipeline 83 simultaneously and connected described hydrodesulphurisatioreactors reactors by the 4th pump 87;
The tower top outlet of described stripping tower 11 connects return tank 12, the gaseous phase outlet of described return tank 12 connects the absorbing-stabilizing system of catalytic cracking unit, the liquid-phase outlet of described return tank returns described stripping tower 11 by the 3rd pump 86, and the sewage outlet of described return tank connects downstream wastewater treatment unit; The bottom of described stripping tower is provided with reboiler, and the heat source passages of described reboiler connects low-pressure steam transport pipe.
Full cut catalytic gasoline selective hydrogenation desulfurization process corresponding to this device comprises the steps:
First the stock oil that temperature is 40 DEG C, pressure is 0.3MPaG enter the particle that strainer 13 filtering is greater than 25 μm, under stock oil surge tank 9 Liquid level, incoming stock oily surge tank 9 carries out deposition dehydrating, in stock oil surge tank 9, logical nitrogen carries out sealing gland, to prevent stock oil ingress of air from causing diolefine oxypolymerization, alleviate the coking of hydrodesulphurisatioreactors reactors top and pressure drop rise.Stock oil after dehydration is sent in First Heat Exchanger 51 and from after the treated gasoline heat exchange of stripping tower 11 by the first pump 84, with the first hydrogen mixing that pressure is 2.0-3.0MPaG, the mixed volume throughput ratio of stock oil and the first hydrogen is 1:30-70, be 1:40-60 preferably, the present embodiment is 1:50; Then to enter in the second interchanger 52 with the three anti-product heat exchange from hydro-sweetening reactor to 120-220 DEG C, enter in dialkene removal reactor 1 after 130-200 DEG C preferably, react at dialkene removal catalyst action.The air speed controlling reaction mass is 2-3/ hour, reaction pressure is 2.5MPaG, is interval with the first beds and the second beds in dialkene removal reactor 1 from top to bottom; Stock oil enters the second beds after the first catalyst bed reaction together with the second hydrogen filled into; The second hydrogen that temperature is 90-100 DEG C, pressure is 2-3MPaG is filled at the middle part of dialkene removal reactor, the amount of filling into of the second hydrogen regulates according to the second beds temperature in, makes the second beds temperature in than the low 5-15 DEG C of the first beds temperature out; The amount of filling into of the present embodiment second hydrogen is 3000Nm
2/ h.
The 3rd hydrogen that the anti-product sent from dialkene removal reactor bottom and temperature are 150-200 DEG C mixes, and the volume flow ratio of an anti-product and the 3rd hydrogen is 1:300-400, and the present embodiment is 1:350.Entering after both mixing in the 3rd interchanger 53 and from delivering in hydrodesulphurisatioreactors reactors 2 after three anti-product heat exchange of sweetening reaction device, under Hydrobon catalyst effect, carrying out desulfurization and some olefin saturated reaction; Fill into first burst of product oil at the middle part of described hydrodesulphurisatioreactors reactors, the amount of filling into of described first burst of product oil is 10t/h.The material inlet temperature controlling hydrodesulphurisatioreactors reactors is 250-350 DEG C, and preferred 280-320 DEG C, in hydrodesulphurisatioreactors reactors, material air speed is 2-3/ hour, and reaction pressure is 2.3MPaG.
Send into hydro-sweetening reactor from top after the first channel that send bottom hydrodesulphurisatioreactors reactors two anti-products enter process furnace 3 is heated to 350-400 DEG C, mercaptan hydrogenolysis occurs under hydro-sweetening catalyst action; Controlling material air speed in hydro-sweetening reactor is 2-3/ hour, reaction pressure 2.0MPaG.
The three anti-products sent from hydro-sweetening reactor bottom enter in the 3rd interchanger 53, second interchanger 52 and the 4th interchanger 54 after heat exchange successively, then enter in product separation device 10 after the first condenser 61 is condensed to 40 DEG C and carry out Oil, Water, Gas three phase separation.Isolated gas phase is condensed to 40 DEG C through the second condenser 62, enter de-hydrocarbon in cyclone separator 8, then enter circulation desulfurization tower 7, absorb with the lean solvent counter current contact entered in circulation desulfurization tower 7, remove the hydrogen sulfide carried secretly in material, the rich solution after washing sends to downstream unit process.
Recycle hydrogen after washing from desulphurization of recycle hydrogen column overhead first block of column plate out, tangentially enter cyclone pipe, the microlayer model carried secretly in recycle hydrogen accelerates to rotate along the helical of cyclone pipe, helical is rotate downward runner, drop also moves downward along helical while rotation, be separated with recycle hydrogen, microlayer model collects the large drop of formation gradually, discharges from the lower nozzle of cyclone pipe.Recycle hydrogen, under the promotion of pressure difference, from the discharge suitable for reading of cyclone pipe, is then discharged via gaseous phase outlet.Lean solvent to enter in tower body above fluid-tight dish from absorption liquid entrance, rests on fluid-tight dish, forms effective fluid-tight to cyclone pipe, when hydrops reach a certain height, overflowed on the seal pot of the first layer column plate by thrust-augmenting nozzle.
Through this desulphurization of recycle hydrogen tower process, compared to prior art, the loss of amine liquid reduces 64%, and recycle hydrogen molecular weight reduces by 0.8; The MDEA content of device outlet be less than 10 micrograms/gram, finally achieve being separated of gas and liquid, can more than 90% be reached to the drop decreasing ratio of more than 15 μm, meet production technique completely to the requirement of recycle hydrogen amine liquid entrainment.
Send to gas-liquid separator 6 after hydrogen after de-hydrocarbon dehydration mixes with fresh hydrogen to isolate liquid phase and send to compressor compresses to 2.0-3.0MPaG, access to plant recycles.
The isolated liquid phase of product separation device 10 sends to downstream wastewater treatment unit; Isolated oil phase enters the 4th interchanger 54 heat exchange, delivers to stripping tower and remove hydrogen sulfide after reclaiming heat.
The tower top temperature controlling described stripping tower is 80-120 DEG C, and stripping pressure is 0.3-0.4MPaG.At the bottom of the tower of stripping tower, obtain treated gasoline, treated gasoline is condensed to 40 DEG C through the 4th condenser 64, sends out-of-bounds as processed oil after entering First Heat Exchanger 51 and stock oil heat exchange by the second pump 85.The gas phase sent from stripper overhead enters in return tank 12 after the 3rd condenser 63 is condensed to 40 DEG C carries out Oil, Water, Gas three phase separation, isolated oil phase returns stripping tower by the 3rd pump 86 and continues process, isolated aqueous phase sends to waste disposal plant, isolated gas phase is sent to catalytic cracking unit and is reclaimed lighter hydrocarbons, can improve liquid total recovery.
The working pressure 0.3-0.4MPaG of stripping tower, is about the half of prior art, effectively reduces the consumption of steam, and energy conservation and consumption reduction effects is remarkable, and the product liquid rate of recovery is high simultaneously.
The present embodiment adopts three reactors in series operations, and First is dialkene removal reactor, and second is hydrodesulphurisatioreactors reactors, and the 3rd is sweetening reaction device; The process furnace of this technique is located at hydrodesulphurisatioreactors reactors outlet, and reaction effluent heats up afterwards and reaction feed heat exchange, and indirect heating reaction feed is to alleviate coking; Process furnace adopts vertical heat exchanging structure, enhancement of heat transfer effect, improves heat transfer efficiency.Especially the design of cyclone separator and desulphurization of recycle hydrogen tower special construction, can the hydrocarbon of entrained with and amine liquid in the isolated gas phase hydrogen of effective elimination, thoroughly avoids the generation of catalyst reactor intoxicating phenomenon; Stripping section adopts single tower low pressure stripping flow process, and reboiler adopts low-pressure steam as thermal source, and compared with passing into the stripping mode at the bottom of tower with employing water vapor, the copper corrosion qualification rate stability of treated gasoline improves, and can reach 100%.
By the present embodiment and Prime-G
+compare with OCT-MD technology, energy consumption consumes as shown in table 1.
Table 1
For the device that scale is 500,000 tons/year, the utility model gross investment about 1.16 ten thousand yuan, after-tax internal rate of return 20%, about 5 years payback periods, project has good profitability; In raw material, sulfur-bearing is 450mg/kg, when requiring that product sulphur content reaches 10mg/kg, can reduce vehicle exhaust SO every year
2quantity discharged 440 tons, significant to protection of the environment.Meanwhile, this technique while sulphur content ≯ 10mg/kg index, can make gasoline octane rating loss reach low-down level, △ RON ≯ 0.7 unit after guarantee gasoline hydrodesulfurizationmethod.
Claims (2)
1. a full cut catalytic gasoline selective hydrodesulfurization device, is characterized in that comprising:
The strainer (13) be connected successively with stock oil pipeline and stock oil surge tank (9), the outlet at bottom of stock oil surge tank connects the first channel entrance of First Heat Exchanger (51) by the first pump (84), first channel outlet connection first connecting tube (81) of described First Heat Exchanger (51), be connected the first channel of the second interchanger (52) after described first connecting tube (81) is connected with the first Hydrogen Line (91) again, the first channel of the second interchanger (52) connects the material inlet of dialkene removal reactor;
The material outlet connection outlet pipeline of described dialkene removal reactor, outlet conduit connects the first channel of the 3rd interchanger (53), and the first channel outlet of described 3rd interchanger (53) connects the material inlet of hydrodesulphurisatioreactors reactors (2);
The material outlet of described hydrodesulphurisatioreactors reactors connects the material inlet of hydro-sweetening reactor (4) by the first channel of process furnace (3), the material outlet of described hydro-sweetening reactor (4) connects the second passage of described 3rd interchanger (53), the second passage of described second interchanger (52), the second passage of the 4th interchanger (54) and the first condenser (61) successively, then connects the material inlet of product separation device (10);
The gaseous phase outlet of described product separation device (10) connects cyclone separator (8) by the second condenser (62), the outlet of described cyclone separator (8) connects the material inlet of circulation desulfurization tower (7), the material outlet of described circulation desulfurization tower (7) connects new hydrogen pipeline (95) by the 4th Hydrogen Line (94), then enters gas-liquid separator (6) together;
The gaseous phase outlet of described gas-liquid separator (6) connects compressor (5), and the outlet of compressor (5) connects described first Hydrogen Line (91), the second Hydrogen Line (92) and the 3rd Hydrogen Line (93) respectively; Described 3rd Hydrogen Line (93) connects the outlet conduit of described dialkene removal reactor (1) by the second passage of described process furnace (3); Described second Hydrogen Line (92) connects the intermediate raw material entrance of described dialkene removal reactor;
The oil phase outlet of described product separation device (10) connects the second passage of described 4th interchanger (54) by second pipe (82), then enter the material inlet of stripping tower (11); The oil phase outlet of described product separation device (10) also connects the 3rd pipeline (83) simultaneously, and the 3rd pipeline (83) connects the intermediate raw material entrance of described hydrodesulphurisatioreactors reactors by the 4th pump (87);
The tower top outlet of described stripping tower (11) connects return tank (12), the gaseous phase outlet of described return tank (12) connects the absorbing-stabilizing system of catalytic cracking unit, the liquid-phase outlet of described return tank returns described stripping tower (11) by the 3rd pump (86), and the sewage outlet of described return tank connects downstream wastewater treatment unit; The bottom of described stripping tower is provided with reboiler, and the heat source passages of described reboiler connects low-pressure steam transport pipe.
2. full cut catalytic gasoline selective hydrodesulfurization device according to claim 1, it is characterized in that the inherent top of tower tray of the tower body of described circulation desulfurization tower (7) and the below of absorption liquid entrance are provided with fluid-tight dish (72), fluid-tight dish (72) is provided with the breach (721) for entering for checking maintenance personnel; The upper cover position of tower body is also provided with the tube sheet (73) for installing cyclone pipe (75), and described tube sheet and cyclone pipe (75) are for removably connecting; Position corresponding to breach (721) is provided with manhole (74) on tower body (71); Described cyclone pipe (75) has many, and the upper end of cyclone pipe (75) is connected on tube sheet (73), and the upper port of cyclone pipe (75) is stretched out tube sheet (73) and exposed; The lower port of cyclone pipe is positioned at the top of described fluid-tight dish (72); Described fluid-tight dish (72) is also provided with the thrust-augmenting nozzle (76) for being imported to by the hydrops of fluid-tight dish (72) top on the seal pot (713) of column plate, the outlet of described thrust-augmenting nozzle (76) is positioned at the below of fluid-tight dish (72) and the seal pot (713) of subtend column plate; The entrance of thrust-augmenting nozzle (76) is positioned at the top of fluid-tight dish (72), and the entrance of thrust-augmenting nozzle (76) is higher than the outlet of described cyclone pipe (75).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420869127.2U CN204385135U (en) | 2014-12-31 | 2014-12-31 | Full cut catalytic gasoline selective hydrodesulfurization device |
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| CN201420869127.2U CN204385135U (en) | 2014-12-31 | 2014-12-31 | Full cut catalytic gasoline selective hydrodesulfurization device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111434754A (en) * | 2019-01-11 | 2020-07-21 | 中国石化工程建设有限公司 | Superposed oil hydrogenation device and superposed oil hydrogenation method |
| CN113952752A (en) * | 2021-10-28 | 2022-01-21 | 镇海石化工程股份有限公司 | Anti-corrosion condensation method for tower top of acidic water stripping device |
-
2014
- 2014-12-31 CN CN201420869127.2U patent/CN204385135U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111434754A (en) * | 2019-01-11 | 2020-07-21 | 中国石化工程建设有限公司 | Superposed oil hydrogenation device and superposed oil hydrogenation method |
| CN113952752A (en) * | 2021-10-28 | 2022-01-21 | 镇海石化工程股份有限公司 | Anti-corrosion condensation method for tower top of acidic water stripping device |
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