CN212127801U - Coal gasification ash water is with removing hard device - Google Patents
Coal gasification ash water is with removing hard device Download PDFInfo
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- CN212127801U CN212127801U CN202020371109.7U CN202020371109U CN212127801U CN 212127801 U CN212127801 U CN 212127801U CN 202020371109 U CN202020371109 U CN 202020371109U CN 212127801 U CN212127801 U CN 212127801U
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Abstract
The utility model belongs to a hardness removal device for coal gasification ash water; the device comprises a gasification clarifying tank and a gasification ash water tank, wherein the gasification clarifying tank is connected with an inlet of a hardness removal reaction tank through a pipeline mixer and an aeration ring, the hardness removal reaction tank is connected with a sedimentation tank, a supernatant outlet of the sedimentation tank is connected with a water production tank through a sand filtering unit, a decarbonizer, a decarbonization water tank and a cation resin exchange unit in sequence, and the water production tank is connected with the gasification ash water tank through a pipeline; a fan is arranged at the bottom of the decarbonizing device; the method has the advantages of simplifying the reagent adding flow, reducing the occupied area of the hardness removing device, effectively removing calcium and magnesium ions in produced water on the premise of not introducing sodium ions and chloride ions, and enabling the grey water to meet the use requirement of a returned gasification grey water system.
Description
Technical Field
The utility model belongs to the technical field of coal gasification water treatment, concretely relates to coal gasification ash water is with removing hard device.
Background
The gasification grey water generally refers to complex water quality obtained after two-stage or three-stage flash evaporation in a gasification slag water treatment process, the gasification grey water is generally high in hardness and turbidity, the hardness mainly exists in a calcium hard form, and a gasification grey water system needs continuous pollution discharge to stabilize the water quality of the system and slow down system scaling. The conventional ash water hardness removal process is to remove the hardness of the ash water by newly building a hardness removal device and using agents such as sodium hydroxide, calcium hydroxide, sodium carbonate and the like, and adjust the pH of the water after hardness removal to be neutral by using hydrochloric acid or sulfuric acid. After the grey water is subjected to a series of treatments, the conductivity is increased, the salt content is increased, the grey water is rich in sodium ions and chloride/sulfate radical ions, the grey water cannot be returned to a gasification cycle for use, and only the grey water can be discharged to a sewage treatment terminal, so that the grey water treatment system cannot really benefit while the treatment cost of the waste water is increased.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the defect among the prior art, and provide a simplify the medicament and add the flow, reduce the device area that removes hard, can effectively get rid of calcium magnesium ion in the product water and make grey water satisfy the coal gasification ash water that returns gasification grey water system operation requirement and use hard device for grey water under the prerequisite of not introducing sodium ion and chloride ion.
The purpose of the utility model is realized like this: a hardness removing device for coal gasification ash water comprises a gasification clarifying tank and a gasification ash water tank, wherein the gasification clarifying tank is connected with an inlet of a hardness removing reaction tank through a pipeline mixer and an aeration ring, the hardness removing reaction tank is connected with a settling tank, a supernatant outlet of the settling tank is connected with a water producing tank through a sand filtering unit, a decarbonizer, a decarbonization water tank and a cation resin exchange unit in sequence, and the water producing tank is connected with the gasification ash water tank through a pipeline; and a fan is arranged at the bottom of the decarbonizing device.
Preferably, the liquid phase inlet of the pipeline mixer is connected with the alkali tank.
Preferably, the outer side of the aeration ring is connected with a carbon dioxide storage tank through a carbon dioxide pipeline, a plurality of aeration branch pipes are uniformly distributed on the inner side of the aeration ring, the inner parts of the aeration branch pipes are communicated with the pipeline, and the outer parts of the aeration branch pipes are connected with the pipeline in a welding manner.
Preferably, a stirring shaft with stirring blades is arranged inside the hardness removing reaction tank, and the top of the stirring shaft is connected with a main shaft of a stirring motor through a coupler.
Preferably, one side of the inner lower part of the hardness removal reaction tank is communicated with a sedimentation tank, a mud scraper is arranged at the inner bottom of the sedimentation tank, and the mud scraper is connected with a belt filter arranged outside the sedimentation tank.
Preferably, the sand filtration unit comprises at least one group of sand filtration parts, each sand filtration part comprises a sand filter, the top of each sand filter is connected with a supernatant outlet of the sedimentation tank through a first tee joint and a first valve, the bottom of each sand filter is connected with the decarbonizer through a second tee joint and a second valve, the third end of each first tee joint is connected with a reflux port at the top of the hardness removal reaction tank through a third valve, the third end of each second tee joint is connected with the third end of each third tee joint through a fourth valve, and a third tee joint is arranged on a pipeline between the water production tank and the gasification ash water tank; and a water production pump is arranged between the water production tank and the third tee joint.
Preferably, the sand filtration unit comprises two sand filtration parts which are arranged in parallel, and a sand filtration water pump is arranged between the sand filtration unit and the decarbonizing device.
Preferably, the cation resin exchange unit comprises at least one cation resin exchange part, the cation resin exchange part comprises a cation resin exchanger, the top of the cation resin exchanger is connected with the decarburization water tank through a fourth tee joint and a fifth valve, and the bottom of the cation resin exchanger is connected with the water production pool through a fifth tee joint and a sixth valve; the third end of the fourth tee joint is connected with the inlet of the brine electrolyzer through a seventh valve, and the third end of the fifth tee joint at the bottom of the cation resin exchanger is connected with the outlet of the acid tank through an eighth valve; and an acid outlet pipeline of the brine electrolyzer is connected with an inlet of the acid tank.
Preferably, the cation resin exchange units are two cation resin exchange parts arranged in parallel, and a decarburization water pump is arranged between the cation resin exchange units and the decarburization water tank.
Preferably, an alkali outlet pipeline of the brine electrolyzer is connected with an inlet of the alkali tank.
The utility model has the advantages of simplify the medicament and add the flow, reduce and remove hard device area, can effectively get rid of calcium magnesium ion in the product water and make grey water satisfy and return gasification grey water system operation requirement under the prerequisite of not introducing sodium ion and chloride ion.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic structural view of the aeration ring of the present invention.
Detailed Description
In order to clearly understand the technical features, objects, and effects of the present invention, embodiments of the present invention will be described with reference to the accompanying drawings, in which like reference numerals refer to like parts in the drawings. For the sake of simplicity, only the parts related to the utility model are schematically shown in the drawings, and they do not represent the actual structure as a product.
As shown in fig. 1 and 2, the utility model relates to a coal gasification ash water is with removing hard device, should remove hard device and include gasification clarifier 1 and gasification ash water tank 2, gasification clarifier 1 passes through pipe mixer 13 and aeration ring 14 and links to each other with the import that removes hard reaction tank 3, removes hard reaction tank 3 and links to each other with sedimentation tank 4, and the supernatant outlet of sedimentation tank 4 loops through sand filtration unit, decarbonizer 7, decarbonization water tank 8 and cation resin exchange unit and links to each other with product water tank 9, and product water tank 9 passes through the pipeline and links to each other with gasification ash water tank 2; the bottom of the decarbonizer 7 is provided with a fan 35. Through setting up the line mixer 13 and the aeration ring 14 not only can conveniently add alkali and carbon dioxide, can also the area of energy-conserving equipment, through setting up sand filtration unit, decarbonization water tank 8 and cation resin exchange unit, can realize getting rid of the hardness content of gasification buck, reduce grey water turbidity and grey water conductivity, further can realize making the grey water satisfy the characteristics that return gasification grey water system operation requirement.
Further, the liquid phase inlet of the line mixer 13 is connected to the alkali tank 12. Pipeline mixer 13 includes two liquid phase imports and mixed liquid outlet, one of them liquid phase import is linked together with gasification clarifier 1, and another liquid phase import is linked together with alkali jar 12, and gasification grey water and alkali are mixed the back and are discharged pipeline mixer 13 through mixed liquid outlet, not only can make gasification grey water and alkali intensive mixing through pipeline mixer 13, can also effectively reduce the area of equipment.
Furthermore, the outer side of the aeration ring 14 is connected with the carbon dioxide storage tank 15 through a carbon dioxide pipeline, a plurality of aeration branch pipes 33 are uniformly distributed on the inner side of the aeration ring 14, the inner parts of the aeration branch pipes 33 are communicated with the pipeline, and the outer parts of the aeration branch pipes 33 are connected with the pipeline in a welding manner. Through the arrangement, the traditional aeration tank structure is changed, the floor area of aeration equipment is reduced, and the aeration efficiency can be improved.
Further, a stirring shaft 16 with stirring blades is arranged inside the hardness removing reaction tank 3, and the top of the stirring shaft 16 is connected with a main shaft of a stirring motor through a coupler. Through setting up above-mentioned agitated vessel can fully stir grey water to reach the purpose of effectively deposiing in the sedimentation tank.
Furthermore, one side of the inner lower part of the hardness removal reaction tank 3 is communicated with the sedimentation tank 4, a mud scraper 18 is arranged at the inner bottom of the sedimentation tank 4, and the mud scraper 18 is connected with a belt filter 19 arranged outside the sedimentation tank 4. One side of the inner lower part of the hardness removal reaction tank 3 is communicated with a sedimentation tank 4, and the grey water is precipitated in the sedimentation tank and is conveyed to a belt filter 19 by a mud scraper 18 for discharging.
Further, the sand filtering unit comprises at least one group of sand filtering parts, each sand filtering part comprises a sand filter 5, the top of each sand filter 5 is connected with a supernatant outlet of the settling pond 4 through a first tee joint 17 and a first valve 20, the bottom of each sand filter 5 is connected with the decarbonizer 7 through a second tee joint 21 and a second valve 22, the third end of the first tee joint 17 is connected with a return port at the top of the hardness removal reaction pond 3 through a third valve 23, the third end of the second tee joint 21 is connected with the third end of a third tee joint 25 through a fourth valve 24, and a third tee joint 25 is arranged on a pipeline between the water production pond 9 and the gasification ash water tank 2; a water producing pump 36 is arranged between the water producing tank 9 and the third tee 25. Through the arrangement, not only can the filtration of suspended particles and impurities in the grey water be realized, but also the convenience is provided for backwashing, the maintenance difficulty and the maintenance strength can be reduced in the actual production process, and the service life of the filtering component can be effectively prolonged.
Further, the sand filtration unit comprises two sand filtration parts which are arranged in parallel, and a sand filtration water pump 28 is arranged between the sand filtration unit and the decarbonizer 7. By arranging the two sand filtering parts, the purpose of synchronously filtering and backwashing can be realized, so that the aims of improving the working efficiency and continuously treating the gasified grey water are fulfilled.
Further, the cation resin exchange unit comprises at least one cation resin exchange part, the cation resin exchange part comprises a cation resin exchanger 6, the top of the cation resin exchanger 6 is connected with the decarburization water tank 8 through a fourth tee 26 and a fifth valve 27, and the bottom of the cation resin exchanger 6 is connected with the water production tank 9 through a fifth tee 29 and a sixth valve 30; the third end of the fourth tee 26 is connected with the inlet of the brine electrolyzer 10 through a seventh valve 31, and the third end of the bottom fifth tee 29 of the cation resin exchanger 6 is connected with the outlet of the acid tank 11 through an eighth valve 32; the acid outlet pipeline of the brine electrolyzer 10 is connected with the inlet of the acid tank 11. Cation exchange resin is filled in the cation resin exchanger 6, and sodium ions in the grey water are absorbed and removed by the cation exchange resin in the cation resin exchanger 6; when the cation exchange resin needs to be regenerated, hydrochloric acid in the acid tank 11 enters the cation resin exchanger 6 for regeneration, brine is generated after regeneration, the brine enters the brine electrolyzer 10 for electrolysis to generate dilute alkali liquor and dilute hydrochloric acid, and the dilute hydrochloric acid enters the acid tank 11 for recycling, so that the recycling of the hydrochloric acid can be realized, and the service life of the cation exchange resin is prolonged.
Furthermore, the cation resin exchange units are two cation resin exchange parts which are arranged in parallel, and a decarburization water pump 34 is arranged between the cation resin exchange units and the decarburization water tank 8.
Further, an alkali outlet pipeline of the brine electrolyzer 10 is connected with an inlet of an alkali tank 12. The dilute alkali liquor generated by electrolyzing the saline water entering the saline water electrolyzer 10 can enter the alkali tank 12 to be used as the alkali liquor, so that the purpose of saving the use amount of the alkali liquor is achieved.
The utility model discloses a theory of operation does: the method comprises the following steps: the gasification grey water from the gasification clarifying tank 1 passes through a pipeline mixer 13 and an aeration ring 14 and then enters a hardness removal reaction tank 3, the hardness of the gasification grey water is 1000-1600mg/L, the turbidity is 15-30NTU, and the conductivity is 3000-5000 us/cm; the alkali liquor in the alkali tank 12 enters a pipeline mixer 13, the mass concentration of the alkali liquor is 10% -20%, the alkali liquor is purchased partially, part of the alkali liquor can be the alkali liquor obtained by a brine electrolyzer 10, the dilute alkali liquor can be dilute sodium hydroxide solution, and the alkali liquor: the ratio of the grey water is 2.5-4L: and 1m carrying out labor intensity. The pH value of the grey water after the alkali liquor is added is 10.5-12.5; the aeration ring 14 is welded with the pipeline through an aeration branch pipe 33, the number of the aeration branch pipes is 4-6, carbon dioxide gas is introduced into the aeration ring 14, and the pH value of grey water after the carbon dioxide gas is introduced is 8.5-9.5. Step two: and after entering the hardness removal reaction tank 3, the grey water is uniformly mixed, fully reacted and then enters the sedimentation tank 4 for sedimentation. Step three: the lower part of the sedimentation tank 4 is provided with a mud scraper 18, and the mud scraper 18 sends the bottom mud into a belt filter 19 for treatment. Step four: and the supernatant of the sedimentation tank 4 enters one of the sand filters 5 to filter and remove suspended particles and impurities in the water, and fine sand particles are contained in the sand filter 5. The two sand filters 5 are arranged in parallel and used alternately; when one of the sand filters 5 is used, back washing is realized through pure produced water in the water producing tank 9, back washing water returns to the hardness removing reaction tank 3, the back washing period of the sand filter is 2-3 times per week, and the back washing time of each time is 20-40 min. Step five: the grey water is filtered by a sand filter 5 and then is sent to a decarbonizer 7 through a sand filter pump 28; the turbidity of the grey water after being filtered by the sand filter 5 is 0.5 to 5 NTU; step six: the bottom of the decarbonizer 7 is provided with a fan 35 in a matching way, the fan 35 is started, carbon dioxide dissolved in grey water is taken out by air generated by the fan 35, and the grey water enters the decarbonization water tank 8. Step seven: the decarbonization water pump 34 pumps the decarbonization grey water in the decarbonization water tank 8 into the cation resin exchanger 6, the cation resin exchanger is filled with cation exchange resin, and sodium ions in the grey water are adsorbed and removed; the two cation resin exchangers 6 are arranged in parallel and used alternately; when the use is finished and the regeneration is needed, the hydrochloric acid in the acid tank 11 enters the cation resin exchanger 6 for regeneration, the brine is generated after the regeneration, the brine enters the brine electrolyzer 10 for electrolysis to generate dilute alkali liquor and dilute hydrochloric acid, the dilute hydrochloric acid enters the acid tank 11 for recycling, and the dilute alkali liquor can enter the alkali tank 12 for recycling; step eight: the grey water enters a production pool 9 after passing through a cation resin exchanger, the grey water in the production pool 9 is pumped back to the gasification grey water tank 2 by a water production pump 39, and the water production pump 39 intermittently transmits backwash water to the sand filter 5 according to the backwashing period of the sand filter. The hardness of the produced water entering the gasification ash water tank 2 is 400mg/L, the turbidity is 0.5-5NTU, the conductivity of the ash water of the water production pool is 3500us/cm, sodium ions and chloride ions are not introduced while calcium and magnesium ions are removed from the produced water, and the produced water is completely returned to the gasification ash water system for recycling.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected," "connecting," and the like are to be construed broadly, and may be, for example, fixedly connected, integrally connected, or detachably connected; or communication between the interior of the two elements; they may be directly connected or indirectly connected through an intermediate, and those skilled in the art can understand the specific meaning of the above terms in the present invention according to the specific situation. The above examples are only specific illustrations of feasible embodiments of the present invention, and they are not intended to limit the scope of the present invention, and all equivalent embodiments, modifications and alterations without departing from the technical spirit of the present invention are intended to be included in the scope of the present invention.
Claims (10)
1. The utility model provides a coal gasification is except that hard device for grey water, this remove hard device includes gasification clarifier (1) and gasification ash basin (2), its characterized in that: the gasification clarifying tank (1) is connected with an inlet of a hardness removal reaction tank (3) through a pipeline mixer (13) and an aeration ring (14), the hardness removal reaction tank (3) is connected with a sedimentation tank (4), a supernatant outlet of the sedimentation tank (4) is connected with a water production tank (9) through a sand filtering unit, a decarbonizer (7), a decarbonization water tank (8) and a cation resin exchange unit in sequence, and the water production tank (9) is connected with the gasification grey water tank (2) through a pipeline; and a fan (35) is arranged at the bottom of the decarbonizer (7).
2. The apparatus of claim 1, wherein: and a liquid phase inlet of the pipeline mixer (13) is connected with the alkali tank (12).
3. The apparatus of claim 1, wherein: the outer side of the aeration ring (14) is connected with a carbon dioxide storage tank (15) through a carbon dioxide pipeline, a plurality of aeration branch pipes (33) are uniformly distributed on the inner side of the aeration ring (14), the inner parts of the aeration branch pipes (33) are communicated with the pipeline, and the outer parts of the aeration branch pipes (33) are connected with the pipeline in a welding mode.
4. The apparatus of claim 1, wherein: the inside of except that hard reaction tank (3) is equipped with (mixing) shaft (16) of taking stirring vane, and the top of (mixing) shaft (16) is passed through the shaft coupling and is linked to each other with agitator motor's main shaft.
5. The coal gasification grey water hardness removal device according to claim 1 or 4, characterized in that: one side of the inner lower part of the hardness removal reaction tank (3) is communicated with the sedimentation tank (4), a mud scraper (18) is arranged at the inner bottom of the sedimentation tank (4), and the mud scraper (18) is connected with a belt filter (19) arranged outside the sedimentation tank (4).
6. The coal gasification grey water hardness removal device according to claim 1 or 4, characterized in that: the sand filtration unit comprises at least one group of sand filtration part, the sand filtration part comprises a sand filter (5), the top of the sand filter (5) is connected with a supernatant outlet of the sedimentation tank (4) through a first tee joint (17) and a first valve (20), the bottom of the sand filter (5) is connected with the decarbonizer (7) through a second tee joint (21) and a second valve (22), the third end of the first tee joint (17) is connected with a reflux port at the top of the hardness removal reaction tank (3) through a third valve (23), the third end of the second tee joint (21) is connected with the third end of the third tee joint (25) through a fourth valve (24), and a third tee joint (25) is arranged on a pipeline between the water production tank (9) and the gasification ash water tank (2); a water producing pump (36) is arranged between the water producing tank (9) and the third tee joint (25).
7. The apparatus of claim 6, wherein: the sand filtering unit comprises two sand filtering parts which are arranged in parallel, and a sand filtering water pump (28) is arranged between the sand filtering unit and the decarbonizing device (7).
8. The apparatus of claim 1, wherein: the cation resin exchange unit comprises at least one cation resin exchange part, the cation resin exchange part comprises a cation resin exchanger (6), the top of the cation resin exchanger (6) is connected with the decarburization water tank (8) through a fourth tee joint (26) and a fifth valve (27), and the bottom of the cation resin exchanger (6) is connected with the water production pool (9) through a fifth tee joint (29) and a sixth valve (30);
the third end of the fourth tee joint (26) is connected with the inlet of the brine electrolyzer (10) through a seventh valve (31), and the third end of a fifth tee joint (29) at the bottom of the cation resin exchanger (6) is connected with the outlet of the acid tank (11) through an eighth valve (32); the acid outlet pipeline of the brine electrolyzer (10) is connected with the inlet of the acid tank (11).
9. The apparatus of claim 8, wherein: the cation resin exchange units are two cation resin exchange parts which are arranged in parallel, and a decarburization water pump (34) is arranged between the cation resin exchange units and the decarburization water tank (8).
10. The apparatus of claim 8, wherein: and an alkali outlet pipeline of the brine electrolyzer (10) is connected with an inlet of an alkali tank (12).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020371109.7U CN212127801U (en) | 2020-10-12 | 2020-10-12 | Coal gasification ash water is with removing hard device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020371109.7U CN212127801U (en) | 2020-10-12 | 2020-10-12 | Coal gasification ash water is with removing hard device |
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| Publication Number | Publication Date |
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| CN212127801U true CN212127801U (en) | 2020-12-11 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202020371109.7U Active CN212127801U (en) | 2020-10-12 | 2020-10-12 | Coal gasification ash water is with removing hard device |
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| CN (1) | CN212127801U (en) |
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- 2020-10-12 CN CN202020371109.7U patent/CN212127801U/en active Active
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