CN103877846A - Desulfurizing and dedusting device and method - Google Patents
Desulfurizing and dedusting device and method Download PDFInfo
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- CN103877846A CN103877846A CN201310680100.9A CN201310680100A CN103877846A CN 103877846 A CN103877846 A CN 103877846A CN 201310680100 A CN201310680100 A CN 201310680100A CN 103877846 A CN103877846 A CN 103877846A
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Abstract
The invention provides a desulfurizing and dedusting device and a desulfurizing and dedusting method. The invention provides a desulfurizing and dedusting device firstly. The desulfurizing and dedusting device comprises a desulfurizing and dedusting module, a waste liquid processing module and a dehydrating module; the desulfurizing and dedusting module mainly comprises a liquid alkaline tank (11), an absorption tower (3) and a circulation tank (9); the waste liquid processing module mainly comprises a medicating tank (15), a sedimentator (14), an oxidizing tank (17), an external water drainage tank (21), a plant area sewage treatment plant (23) and a filtrate storage tank (19); the dehydrating module mainly comprises a plate-frame-type press filter (25). The invention provides a desulfurizing and dedusting method according to the device. The desulfurizing and dedusting device and method which are provided by the invention have the beneficial effects of low investment, high desulfurizing and dedusting efficiency and short construction cycle and is adaptive to the situation of China.
Description
Technical field
The present invention relates to environmental technology field, relate in particular to a kind of pollution abatement equipment and method, specifically refer to a kind of desulfurating dust-removing equipment and method.
Background technology
National environmental protection " 12 " planning points out, the Industrial Stoves of the industries such as petroleum and petrochemical industry, coloured, building materials will carry out desulfurization transformation.In " 12 " environmental protection leading indicator, sulfur dioxide (SO2) emissions total amount requires 2015 to drop to 2086.4 ten thousand tons, and comparing the range of decrease in 2010 is 8%.At present, the boiler plant desulfurization project of coal-burning power plant of China draws to an end, and therefore reduces refinery catalytic cracking unit's smoke SO 2 discharge and is just receiving unprecedented concern.
Wet method is still the main method that smoke SO 2 removes at present, mainly contains lime stone (lime)-gypsum, two alkaline process, magnesium method, ammonia process etc.The features such as catalytic cracking unit flue gas has that flue-gas temperature high (180 ~ 280 DEG C), dust content are large, smoke content fluctuation range large (150 ~ 500mg/Nm3, the limit can reach 20g/Nm3), flue gas pressures are little, cause traditional wet desulphurization method all inapplicable.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of invest little, desulfurization dust-removing efficiency is high refinery catalytic cracking unit's regeneration flue gas desulfurization cleaner and method.
First technical solution of the present invention provides a kind of desulfurating dust-removing equipment, comprise desulfurization and dedusting module, liquid waste processing module and dehydration module, described desulfurization and dedusting module comprise liquid caustic soda tank and, absorption tower and circulatory pool, the entrance on described absorption tower is provided with contrary spraying nozzle and pre-temperature descending section, described absorption tower is the countercurrent absorber that liquidates, cigarette tower Integral type structure, described absorption tower comprises lower floor's spray from bottom to top successively, the adverse current that liquidates assembly, higher level's spray, demister and chimney, described liquid caustic soda tank is connected to lower floor's spray section below by liquid caustic soda pump, the bottom on described absorption tower is connected to circulatory pool by pipeline, described circulatory pool is connected to respectively lower floor's spray and the adverse current assembly that liquidates by the circulating pump being provided with, the logical former flue gas of entrance on absorption tower, described contrary spraying nozzle connects fresh water, described liquid waste processing module comprises grug feeding jar, settling vessel, oxidation tank, outer blowoff basin, sewage treatment plant of plant area and filtrate tanks, described circulatory pool by positive displacement pump, grug feeding jar by dosing pump be connected to settling vessel, described settling vessel top is provided with overfall and is connected to respectively oxidation tank and filtrate tanks by pipeline, described oxidation tank blasts the bottom of air to oxidation tank by the oxidation fan being provided with, described oxidation tank is connected to outer blowoff basin by overfall, and outer blowoff basin is delivered to sewage treatment plant by the outer draining pump being provided with by sewage, described dehydration module comprises plate and frame filter press, the bottom of described settling vessel is connected with plate and frame filter press by sludge pump, the filtrate of plate and frame filter press is connected to filtrate tanks by pipeline or/and oxidation tank, and described filtrate tanks is returned to pump by filtrate and is connected with circulatory pool.
As preferably, described circulatory pool is also connected with contrary spraying nozzle by circulating pump.
As preferably, described settling vessel is vertical-flow settling vessel.
As preferably, described demister is ridge type demister.
Technical solution of the present invention also provides a kind of desulfurization and dust-removal method, and above-mentioned desulfurating dust-removing equipment, comprises the following steps,
(a) first flue gas enters the pre-temperature descending section desulfurization and dedusting of absorption tower entrance, enters subsequently absorption tower and loop slurry counter current contacting, and by the adverse current assembly deep desulfuration dedusting that liquidates in tower, discharges finally by crossing after demister is removed large drop;
(b) by the liquid caustic soda of the continuous replenishment system internal consumption of liquid caustic soda pump;
(c) slurries in circulatory pool are sent in absorption tower flue gas desulfurization and dedusting under circulating pump effect;
(d) loop slurry constantly absorbs SO2 and the dust in flue gas, and generates the mixed serum of sodium sulfite, sodium hydrogensulfite and dust, drains into sedimentation basin after reaching finite concentration by positive displacement pump;
(e) first mixed serum enters settling vessel, and through enough time of staying, dust sinks to settling vessel bottom, and upper clear supernate enters respectively oxidation tank and filtrate holding vessel;
(f) in oxidation tank, be provided with aerator, in oxidation tank, blast air by oxidation fan, thereby the sodium sulfite in waste liquid and sodium hydrogensulfite are oxidized to sodium sulphate and reduce the COD of waste liquid;
(g) in oxidation tank waste liquid through outer draining pump deliver to sewage treatment plant of plant area or increase sodium sulphate prepare retracting device;
(h) clear liquid in filtrate holding vessel returns to pumped back circulatory pool by filtrate;
(i) the flue dust mud that contains of settling vessel bottom is delivered to plate and frame filter press dehydration by sludge pump, makes filter cake outward transport, can select to enter filtrate tanks and/or oxidation tank from plate and frame filter press filtrate out.
Wherein, desulfurization primer fluid adopts the proportional arrangement that fresh water and 30% sodium hydroxide solution are pressed 3:1.
Wherein, in the described unit interval magnitude of recruitment of 30% sodium hydroxide solution by the ratio of amount be in absorption tower SO2 treating capacity 1.02～1.05.
Wherein, described circulatory pool pH value is controlled at 6～8, and described circulatory pool discharge opeing density is controlled at 1.05～1.2g/cm3, and the liquid-gas ratio of described circulation fluid and flue gas is 4～12L/m3.
Wherein, the oxidization time of described oxidation tank is not less than 6 hours.
Wherein, the mass concentration of the filtrate of described plate and frame filter press discharge is for being no more than 15%, and filter cake moisture content is 30～40%.
Beneficial effect of the present invention is:
(1) equipment is all domestic, has shortened the construction period, is convenient to maintenance.
(2) invest littlely, operating cost is low: adopt tower outer circulation mode, reduced the height on absorption tower, reduced circulating pump lift and power of motor simultaneously; The version of cigarette tower unification has been saved flue material to greatest extent; The pre-cooling of flue gas has been ensured to absorption tower can select lower material.
(3) desulfurization dust-removing efficiency is high: absorption tower adopts the adverse current desulfurizing tower that liquidates, and has ensured higher desulfurization dust-removing efficiency.
The present invention has overcome current catalytic cracking unit flue gas desulfurization technique complexity, has invested the shortcomings such as high, the completion time of project is long, is especially applicable to domestic middle-size and small-size catalytic cracking unit flue gas desulfurization.
Brief description of the drawings
Accompanying drawing 1 is desulfurating dust-removing equipment pipe connecting structure schematic diagram of the present invention;
Shown in figure:
1, pre-temperature descending section, 2, contrary spraying nozzle, 3, absorption tower, 4, lower floor spray, 5, the adverse current that liquidates assembly, 6, higher level's spray, 7, demister, 8, chimney, 9, circulatory pool, 10, circulating pump, 11, liquid caustic soda tank, 12, liquid caustic soda pump, 13, positive displacement pump, 14, settling vessel, 15, grug feeding jar, 16, dosing pump, 17, oxidation tank, 18, oxidation fan, 19, filtrate tanks, 20, filtrate is returned to pump, 21, outer blowoff basin, 22, outer draining pump, 23, sewage treatment plant of plant area, 24, sludge pump, 25, plate and frame filter press.
Detailed description of the invention
Below in conjunction with accompanying drawing 1, the detailed description of the invention of of the present invention pair of desulfurating dust-removing equipment and method is described in detail below, should be understood that following embodiment is to most preferred embodiment of the present invention, not as limitation of the present invention.
As shown in Figure 1, a kind of desulfurating dust-removing equipment, comprise desulfurization and dedusting module, liquid waste processing module and dehydration module, described desulfurization and dedusting module comprises liquid caustic soda tank and 11, absorption tower 3 and circulatory pool 9, the entrance on described absorption tower 3 is provided with contrary spraying nozzle 2 and pre-temperature descending section, described absorption tower 3 is the countercurrent absorber that liquidates, cigarette tower Integral type structure, described absorption tower 3 comprises lower floor's spray 4 from bottom to top successively, the adverse current that liquidates assembly 5, higher level sprays 6, demister 7 and chimney 8, described liquid caustic soda tank is connected to lower floor's spray section below by liquid caustic soda pump, the bottom on described absorption tower 3 is connected to circulatory pool 9 by pipeline, described circulatory pool 9 is connected to respectively lower floor's spray 4 and the adverse current assembly 5 that liquidates by the circulating pump being provided with, the logical former flue gas of entrance on absorption tower, described contrary spraying nozzle 2 connects fresh water, described liquid waste processing module comprises grug feeding jar 15, settling vessel 14, oxidation tank 17, outer blowoff basin 21, sewage treatment plant of plant area 23 and filtrate tanks 19, described circulatory pool 9 is by positive displacement pump 13, grug feeding jar is connected to settling vessel 14 by dosing pump, described settling vessel 14 tops are provided with overfall and are connected to respectively oxidation tank 17 and filtrate tanks 19 by pipeline, described oxidation tank 17 blasts the bottom of air to oxidation tank 17 by the oxidation fan 18 being provided with, described oxidation tank 17 is connected to outer blowoff basin 21 by overfall, outer blowoff basin 21 is delivered to sewage treatment plant 23 by the outer draining pump 22 being provided with by sewage, described dehydration module comprises plate and frame filter press 25, the bottom of described settling vessel 14 is connected with plate and frame filter press 25 by sludge pump 24, the filtrate of plate and frame filter press 25 is connected to filtrate tanks 19 by pipeline or/and oxidation tank 17, and described filtrate tanks 19 is returned to pump 20 by filtrate and is connected with circulatory pool 9.
In the present embodiment, described circulatory pool 9 is also connected with contrary spraying nozzle 2 by circulating pump 10.
Wherein, described settling vessel 14 is vertical-flow settling vessel.
Wherein, described demister is ridge type demister.
The oil plant desulphurizing and dedusting catalytic cracking regenerated smoke method of the present embodiment, design exhaust gas volumn is 100,000 Nm3/h, and SO 2 from fume concentration is 600 ~ 800mg/Nm3, and dust concentration is 150 ~ 300mg/Nm3, and liquid-gas ratio is 8L/m3.Flue gas after treatment sulfur dioxide concentration is down to 20mg/Nm3, and dust concentration is down to 40mg/Nm3, and efflux wastewater amount is 6 ~ 7m3/h, and efflux wastewater COD maintains 7 left and right lower than 80mg/L, SS lower than 60mg/L, PH, completely meet and higher than existing environmental requirement.
The present embodiment specifically comprises the steps:
The present embodiment specifically comprises the steps:
(1) by liquid caustic soda pump 12,30% liquid caustic soda solution in liquid caustic soda tank 11 is sent into circulatory pool 9, add water and be configured to certain density circulation fluid.
(2) by circulating pump 10, circulation fluid is delivered to pre-cool-down nozzle 2, lower floor's spray 4 and upper strata spray 6; First flue gas carries out counter current contacting through pre-temperature descending section 1 and the circulation fluid that pre-cool-down nozzle 2 sprays, lower the temperature and reach capacity after enter absorption tower 3, under 4 effects of lower floor's spray, lower the temperature and desulfurization and dedusting, carry out deep desulfuration dedusting through the adverse current assembly 5 that liquidates subsequently, finally by crossing after upper strata spray 6 and demister 7 through chimney 8 qualified discharges.
(3) circulation fluid constantly absorbs sulfur dioxide and the flue dust in flue gas, sulfur dioxide reacts with liquid caustic soda and generates sodium sulfite solution, reach after finite concentration and pH value, deliver to settling vessel 14 by positive displacement pump 13, by dosing pump 16, the flocculant in grug feeding jar 15 is sent into settling vessel 14.Mixed liquor is interior through Separation of Solid and Liquid at settling vessel 14, is settled down to bottom, and the selective overflow of clear liquid enters oxidation tank 17 and filtrate tanks 19.Settling vessel 14 bottom precipitations are delivered to plate and frame filter press 25 by sludge pump 24, and after press filtration, filter cake falls into the pack outward transport of slag storehouse, and filtrate selectively enters filtrate tanks 19 or oxidation tank 17.
(4) open oxidation fan 18, in oxidation tank 18, blast air, the sodium sulfite in waste liquid is oxidized to sodium sulphate to reduce COD (COD);
(5) waste liquid after oxidation enters blowoff basin 21, finally by outer draining pump 22, waste liquid after treatment is sent into sewage treatment plant of plant area 23;
(6) clear liquid in filtrate tanks 19 returns to pump 20 by filtrate and sends absorption tower 3 back to and recycle;
(7), along with the decline of circulation fluid pH value, need regularly to pass through liquid caustic soda pump 12 to the interior supplementary liquid caustic soda of circulatory pool 9.
The main points of the present embodiment are: 1, in absorption tower, adopted the adverse current assembly that liquidates, compared common spray column and greatly improved efficiency of dust collection.2, circulation fluid pH value is key control parameter, to the control of pH value and desulfurization absorbent feeding coal, should ensure the pH value of circulation fluid within the specific limits, ensures that again the quantity delivered of liquid caustic soda can not be too high, otherwise easily causes the waste of desulfurizing agent.3, the density of circulation fluid is key control parameter, and density Tai Gaoyi causes absorption tower intercrystalline, and the too low desulfuration efficiency of density declines.4, sulfur removal technology adopts personality board frame filtering equipment, by selecting meticulous filter cloth and compression system, in ensureing dewatering efficiency, has greatly saved space and investment.5, absorption tower demisting device adopts ridge type demister, has improved demist efficiency.
Above embodiment is that 1 pair of best detailed description of the invention of the present invention is described by reference to the accompanying drawings, but these explanations can not be understood to limit scope of the present invention, obviously, under design of the present invention, still can make a lot of variations.In this explanation, any any change of making under inventive concept of the present invention all will fall within the scope of protection of the present invention.
Claims (10)
1. a desulfurating dust-removing equipment, is characterized in that: comprise desulfurization and dedusting module, liquid waste processing module and dehydration module,
Described desulfurization and dedusting module comprises liquid caustic soda tank and (11), absorption tower (3) and circulatory pool (9), the entrance on described absorption tower (3) is provided with contrary spraying nozzle (2) and pre-temperature descending section, described absorption tower (3) is the countercurrent absorber that liquidates, cigarette tower Integral type structure, described absorption tower (3) comprises lower floor's spray (4) from bottom to top successively, the adverse current that liquidates assembly (5), higher level sprays (6), demister (7) and chimney (8), described liquid caustic soda tank is connected to lower floor's spray section below by liquid caustic soda pump, the bottom on described absorption tower (3) is connected to circulatory pool (9) by pipeline, described circulatory pool (9) is connected to respectively lower floor spray (4) and the adverse current assembly (5) that liquidates by the circulating pump being provided with, the logical former flue gas of entrance on absorption tower, described contrary spraying nozzle (2) connects fresh water,
Described liquid waste processing module comprises grug feeding jar (15), settling vessel (14), oxidation tank (17), outer blowoff basin (21), sewage treatment plant of plant area (23) and filtrate tanks (19), described circulatory pool (9) is by positive displacement pump (13), grug feeding jar is connected to settling vessel (14) by dosing pump, described settling vessel (14) top is provided with overfall and is connected to respectively oxidation tank (17) and filtrate tanks (19) by pipeline, described oxidation tank (17) blasts the bottom of air to oxidation tank (17) by the oxidation fan (18) being provided with, described oxidation tank (17) is connected to outer blowoff basin (21) by overfall, outer blowoff basin (21) is delivered to sewage treatment plant (23) by the outer draining pump (22) being provided with by sewage,
Described dehydration module comprises plate and frame filter press (25), the bottom of described settling vessel (14) is connected with plate and frame filter press (25) by sludge pump (24), the filtrate of plate and frame filter press (25) is connected to filtrate tanks (19) by pipeline or/and oxidation tank (17), and described filtrate tanks (19) is returned to pump (20) by filtrate and is connected with circulatory pool (9).
2. desulfurating dust-removing equipment according to claim 1, is characterized in that: described circulatory pool (9) is also connected with contrary spraying nozzle (2) by circulating pump (10).
3. desulfurating dust-removing equipment according to claim 1, is characterized in that: described settling vessel (14) is vertical-flow settling vessel.
4. desulfurating dust-removing equipment according to claim 1, is characterized in that: described demister is ridge type demister.
5. a desulfurization and dust-removal method, adopts the desulfurating dust-removing equipment described in claim 1 to 4 arbitrary claim, it is characterized in that: comprise the following steps,
(a) first flue gas enters the pre-temperature descending section of absorption tower (3) entrance (1) desulfurization and dedusting, enter subsequently absorption tower (3) and loop slurry counter current contacting, and by adverse current assembly (5) the deep desulfuration dedusting that liquidates in tower, discharge finally by crossing after demister (7) is removed large drop;
(b) by the constantly liquid caustic soda of replenishment system internal consumption of liquid caustic soda pump (12);
(c) slurries in circulatory pool (9) are sent in absorption tower (3) flue gas desulfurization and dedusting under circulating pump (10) effect;
(d) loop slurry constantly absorbs SO2 and the dust in flue gas, and generates the mixed serum of sodium sulfite, sodium hydrogensulfite and dust, drains into sedimentation basin (14) after reaching finite concentration by positive displacement pump (13);
(e) first mixed serum enters settling vessel (14), and through enough time of staying, dust sinks to settling vessel (14) bottom, and upper clear supernate enters respectively oxidation tank (17) and filtrate holding vessel (19);
(f) in oxidation tank (17), be provided with aerator, in oxidation tank (17), blast air by oxidation fan (18), thereby the sodium sulfite in waste liquid and sodium hydrogensulfite are oxidized to sodium sulphate and reduce the COD of waste liquid;
(g) the middle waste liquid of oxidation tank (17) is delivered to sewage treatment plant of plant area (23) or is increased sodium sulphate through outer draining pump (22) and prepares retracting device;
(h) clear liquid in filtrate holding vessel (19) returns to pump (20) by filtrate and sends circulatory pool (9) back to;
(i) the flue dust mud that contains of settling vessel (14) bottom is delivered to plate and frame filter press (25) dehydration by sludge pump (24), makes filter cake outward transport, can select to enter filtrate tanks (19) or/and oxidation tank (17) from plate and frame filter press (25) filtrate out.
6. sulfur method according to claim 5, is characterized in that: desulfurization primer fluid adopts fresh water and 30% sodium hydroxide solution by the proportional arrangement of 3:1.
7. sulfur method according to claim 5, is characterized in that: in the described unit interval magnitude of recruitment of 30% sodium hydroxide solution by the ratio of amount be in absorption tower SO2 treating capacity 1.02～1.05.
8. sulfur method according to claim 5, is characterized in that: described circulatory pool pH value is controlled at 6～8, and described circulatory pool discharge opeing density is controlled at 1.05～1.2g/cm3, and the liquid-gas ratio of described circulation fluid and flue gas is 4～12L/m3.
9. sulfur method according to claim 5, is characterized in that: the oxidization time of described oxidation tank (17) is not less than 6 hours.
10. sulfur method according to claim 5, is characterized in that: the mass concentration of the filtrate of described plate and frame filter press (25) discharge is for being no more than 15%, and filter cake moisture content is 30～40%.
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| CN201310680100.9A CN103877846B (en) | 2013-12-13 | 2013-12-13 | Desulfurating dust-removing equipment and method |
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| CN104261356A (en) * | 2014-09-09 | 2015-01-07 | 安徽省司尔特肥业股份有限公司 | Dilute acid purification technique |
| CN105126507A (en) * | 2015-10-09 | 2015-12-09 | 江苏正通宏泰股份有限公司 | Ultra-clean dust removal device for desulfurizing tower |
| CN105126501A (en) * | 2015-08-05 | 2015-12-09 | 湖南华银能源技术有限公司 | Method and apparatus for removing fine dust and gas pollutants in flue gas |
| CN107261797A (en) * | 2017-07-07 | 2017-10-20 | 江苏盐环实业有限公司 | A kind of environmentally friendly novel desulphurization equipment for handling waste water and waste gas |
| CN107648978A (en) * | 2017-10-27 | 2018-02-02 | 中冶华天工程技术有限公司 | Wet desulfurization flue gas eliminates plume system and method |
| CN108325381A (en) * | 2018-03-02 | 2018-07-27 | 金鑫来 | A kind of efficient industrial waste gas filter device |
| CN109985503A (en) * | 2019-04-12 | 2019-07-09 | 沁阳市华达实业有限公司 | A kind of glance coal waste gas purification treatment process |
| CN111054207A (en) * | 2020-01-17 | 2020-04-24 | 国惠环保新能源有限公司 | Carbide slag-gypsum flue gas desulfurization device and method applied to multi-tube water bed |
| CN115159469A (en) * | 2022-06-29 | 2022-10-11 | 江苏德义通环保科技有限公司 | Recovering SO with different concentrations from waste liquid 2 Apparatus and method for gas |
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| CN109985503A (en) * | 2019-04-12 | 2019-07-09 | 沁阳市华达实业有限公司 | A kind of glance coal waste gas purification treatment process |
| CN111054207A (en) * | 2020-01-17 | 2020-04-24 | 国惠环保新能源有限公司 | Carbide slag-gypsum flue gas desulfurization device and method applied to multi-tube water bed |
| CN111054207B (en) * | 2020-01-17 | 2024-02-02 | 国惠环保新能源有限公司 | Carbide slag-gypsum flue gas desulfurization device and method applied to multi-pipe water bed |
| CN115159469A (en) * | 2022-06-29 | 2022-10-11 | 江苏德义通环保科技有限公司 | Recovering SO with different concentrations from waste liquid 2 Apparatus and method for gas |
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