CN111153416A - System and method for preparing ammonium sulfate from active coke desulfurization rich gas - Google Patents
System and method for preparing ammonium sulfate from active coke desulfurization rich gas Download PDFInfo
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- CN111153416A CN111153416A CN202010072076.0A CN202010072076A CN111153416A CN 111153416 A CN111153416 A CN 111153416A CN 202010072076 A CN202010072076 A CN 202010072076A CN 111153416 A CN111153416 A CN 111153416A
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- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 title claims abstract description 147
- 229910052921 ammonium sulfate Inorganic materials 0.000 title claims abstract description 147
- 235000011130 ammonium sulphate Nutrition 0.000 title claims abstract description 147
- 239000000571 coke Substances 0.000 title claims abstract description 43
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 43
- 230000023556 desulfurization Effects 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000002002 slurry Substances 0.000 claims abstract description 114
- 238000010521 absorption reaction Methods 0.000 claims abstract description 103
- 238000006243 chemical reaction Methods 0.000 claims abstract description 83
- 238000001035 drying Methods 0.000 claims abstract description 53
- 238000001914 filtration Methods 0.000 claims abstract description 37
- 238000001704 evaporation Methods 0.000 claims abstract description 33
- 230000018044 dehydration Effects 0.000 claims abstract description 32
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 32
- 230000008020 evaporation Effects 0.000 claims abstract description 31
- 238000005507 spraying Methods 0.000 claims abstract description 30
- 239000013078 crystal Substances 0.000 claims abstract description 20
- 230000008929 regeneration Effects 0.000 claims abstract description 20
- 238000011069 regeneration method Methods 0.000 claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000000843 powder Substances 0.000 claims abstract description 12
- 239000012535 impurity Substances 0.000 claims abstract description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 43
- 239000007787 solid Substances 0.000 claims description 13
- 239000000047 product Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 11
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 10
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 10
- 230000001105 regulatory effect Effects 0.000 claims description 9
- 230000003647 oxidation Effects 0.000 claims description 7
- 238000007254 oxidation reaction Methods 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- 239000011343 solid material Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000005406 washing Methods 0.000 claims description 5
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- 239000006228 supernatant Substances 0.000 claims description 4
- 238000004458 analytical method Methods 0.000 claims description 3
- 230000001174 ascending effect Effects 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- 238000001556 precipitation Methods 0.000 claims description 3
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 239000013049 sediment Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 107
- 239000003546 flue gas Substances 0.000 abstract description 21
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 18
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 12
- 239000007921 spray Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000000779 smoke Substances 0.000 description 6
- 239000000428 dust Substances 0.000 description 5
- 238000005245 sintering Methods 0.000 description 5
- 238000004064 recycling Methods 0.000 description 4
- 230000010354 integration Effects 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 230000003750 conditioning effect Effects 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000001166 ammonium sulphate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- ADHFGLVXSIGCIG-UHFFFAOYSA-N diazanium sulfate hydrochloride Chemical compound [NH4+].[NH4+].Cl.[O-]S([O-])(=O)=O ADHFGLVXSIGCIG-UHFFFAOYSA-N 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/245—Preparation from compounds containing nitrogen and sulfur
- C01C1/246—Preparation from compounds containing nitrogen and sulfur from sulfur-containing ammonium compounds
- C01C1/247—Preparation from compounds containing nitrogen and sulfur from sulfur-containing ammonium compounds by oxidation with free oxygen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/22—Sulfites of ammonium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a system and a method for preparing ammonium sulfate from active coke desulfurization rich gas, wherein the system comprises the following steps: reaction system for absorbing SO in the regeneration gas2After reaction, absorption slurry containing ammonium sulfate is generated; the filtering system is used for removing carbon powder and impurities in the slurry to obtain a purified ammonium sulfate solution; the evaporation concentration system is used for carrying out evaporation concentration on the purified ammonium sulfate solution to form ammonium sulfate crystal slurry; the dehydration drying system is used for dehydrating and drying the ammonium sulfate crystal slurry to form an ammonium sulfate powder finished product; and the tail gas treatment system is used for purifying and treating the tail gas generated by the dehydration drying system and the reaction system. According to the inventionThe system and the method adopt a three-stage spraying device to fully absorb SO in the flue gas2The generation rate of ammonium sulfate is increased; the investment cost is reduced, and the cost is low; the ammonium sulfate product can be continuously produced, the water content of the ammonium sulfate is low, and the hardening problem of the finished product is avoided; the system has good circulation.
Description
Technical Field
The invention belongs to the technical field of dry-process activated coke desulfurization and denitrification rich gas recycling in the environmental protection industry, and particularly relates to a system and a method for preparing ammonium sulfate by recycling activated coke desulfurization rich gas.
Background
At present, the atmospheric pollutant treatment measures of steel enterprises in China can be roughly summarized into three categories: 1. basic conditions of raw material control and flue gas emission reduction; 2. an effective means of controlling the sintering process and reducing the emission of flue gas; 3. the final means and the final guarantee of the flue gas treatment. Among the three treatment measures, people often pay more attention to the tail end treatment of the flue gas. At present, the tail end treatment of sintering flue gas mainly comprises active coke desulfurization and denitration integration, flue gas desulfurization (wet method, dry method and semi-dry method), medium-low temperature SCR denitration integration and other technologies.
The integration of flue gas desulfurization (wet method, dry method and semi-dry method) and medium-low temperature SCR denitration is to treat the flue gas at the tail end of the sintering flue gas through a flue gas treatment system and remove harmful substances SO in the flue gas through absorption2And NOx, substances after tail gas absorption treatment can not be recycled; the dry active coke desulfurization and denitrification technology utilizes the active coke to remove SO in the flue gas2And NOx, and resolving the active coke at 450 ℃ to obtain gases with higher concentration, wherein the gases with higher concentration are collectively called active coke regeneration gases, the regeneration gases are desulfurization rich gases of the active coke, and the main components of the regeneration gases are shown in the following table:
regeneration generated by dry-method activated coke desulfurization and denitrification technologyThe gas contains more SO2Gas, absorbing and resolving the active coke to obtain high-concentration SO2Gas, if capable of converting SO in high concentration2The gas is reasonably utilized and used as an industrial preparation raw material to prepare industrial ammonium sulfate hydrochloride, the sintering flue gas is recycled, the environmental pollution is reduced, and the method has important significance for improving the industrial production process.
Therefore, there is a need to provide an improved solution to the above-mentioned deficiencies of the prior art.
Disclosure of Invention
The invention aims to provide a system and a method for preparing ammonium sulfate from active coke desulfurization rich gas, which aim to solve the problems that the utilization rate of sintering flue gas is low, the pollution flue gas cannot be recycled and the resource waste is caused in the current steel production process.
In order to achieve the above purpose, the invention provides the following technical scheme:
a system for preparing ammonium sulfate from active coke desulfurization rich gas comprises:
reaction system for absorbing SO in the regeneration gas2After reaction, absorption slurry containing ammonium sulfate is generated;
the filtering system is connected with a slurry outlet of the reaction system and is used for removing carbon powder and impurities in the slurry to obtain a purified ammonium sulfate solution;
the solution outlet of the filtering system is connected with the inlet of the evaporation concentration system, and the evaporation concentration system is used for carrying out evaporation concentration on the purified ammonium sulfate solution to form ammonium sulfate crystal slurry;
the outlet of the evaporation concentration system is connected with the inlet of the desulfurization drying system, and the dehydration drying system is used for dehydrating and drying the ammonium sulfate crystal slurry to form an ammonium sulfate powder finished product;
and the tail gas treatment system is respectively connected with the dehydration drying system and the tail gas outlet of the reaction system and is used for purifying and treating tail gas generated by the dehydration drying system and the reaction system.
In the system for preparing ammonium sulfate from the active coke desulfurization rich gas, preferably, the reaction system comprises: reaction column for regenerating SO in a gas2The reaction tower is internally provided with a spraying device which is used for spraying absorption slurry, and the ascending regeneration gas and the descending absorption slurry are contacted and reacted to generate ammonium sulfate; an oxidation fan is arranged outside the reaction tower, and a gas outlet of the oxidation fan is connected with an absorption slurry pool at the bottom of the reaction tower and used for oxidizing ammonium sulfite in the absorption slurry into ammonium sulfate;
preferably, the reaction system further comprises a circulating pump, the circulating pump is arranged outside the reaction tower, and the circulating pump circulates the absorption slurry at the bottom of the reaction tower to the upper part of the reaction tower for spraying;
preferably, the spraying devices are multiple, and the multiple spraying devices absorb the regeneration gas layer by layer; the number of the spraying devices is preferably three;
still preferably, the absorption slurry containing ammonium sulfate enters the filtration system when the mass concentration of ammonium sulfate in the absorption slurry containing ammonium sulfate at the bottom of the reaction tower is 20-23%.
In the system for preparing ammonium sulfate from the active coke desulfurization rich gas, preferably, the filtering system comprises a plate-and-frame filter press and a clarifier; the inlet of the plate-and-frame filter press is connected with the slurry outlet of the reaction system, and the inlet of the clarifier is connected with the slurry outlet of the plate-and-frame filter press; returning the sediment at the bottom of the clarifier to the plate-and-frame filter press again for filtering, feeding the absorption slurry containing ammonium sulfate of the reaction system into the plate-and-frame filter press for filtering, feeding the slurry flowing out of the plate-and-frame filter press into the clarifier for precipitation and purification, and obtaining a pure ammonium sulfate solution;
preferably, the clarifier comprises two stages, namely a first-stage clarifier and a second-stage clarifier, wherein an overflow port of the first-stage clarifier is connected with an inlet of the second-stage clarifier;
preferably, a regulating box is arranged between the reaction system and the filtering system, and slurry from the reaction system enters the regulating box firstly and then enters the filtering system;
still preferably, the filtration system further comprises a buffer tank into which overflow liquid of the secondary clarifier enters.
In the above system for preparing ammonium sulfate from active coke desulfurization rich gas, preferably, the evaporation concentration system comprises:
the heater comprises a tube pass and a shell pass, the tube pass is used for storing slurry, the shell pass is used for storing hot steam, and the heater is connected with a slurry outlet of the buffer tank and is used for heating, evaporating and concentrating an ammonium sulfate solution to form ammonium sulfate crystal slurry;
the inlet of the separator is connected with the tube pass outlet of the heater, the separator is used for carrying out gas-liquid separation on the ammonium sulfate crystal slurry, and the bottom circulating slurry outlet of the separator is connected to the tube pass bottom inlet of the heater through an evaporation circulating pump, so that the slurry is continuously circulated and evaporated; the bottom concentrated slurry outlet of the separator is connected with the dehydration drying system;
the condenser is used for cooling the steam from the separator and the heater;
the vacuum pump is connected with the condenser and enables negative pressure to be formed in the condenser; preferably also creating a negative pressure within the separator;
preferably, the vacuum pump is connected to the vacuum tank, and both a top outlet and a bottom outlet of the condenser are connected to the vacuum tank.
The system for preparing the ammonium sulfate from the active coke desulfurization rich gas preferably comprises a cyclone, a centrifugal device and a drying device;
the inlet of the cyclone is connected with the slurry outlet of the evaporation concentration system and is used for carrying out solid-liquid separation and dehydration on the ammonium sulfate slurry; a bottom slurry outlet of the cyclone is connected with an inlet of the centrifugal device for further dehydration, and a solid material containing the ammonium sulfate is recovered; the drying device is connected with a solid outlet of the centrifugal device and is used for drying the solid material containing the ammonium sulfate;
preferably, the upper liquid outlet of the cyclone and the supernatant outlet of the centrifuge are both connected to the reaction system.
In the system for preparing ammonium sulfate from the active coke desulfurization rich gas, preferably, the drying device comprises a fluidized bed and a cyclone collector, a gas outlet of the fluidized bed and a gas outlet of the centrifugal device are both connected with an inlet of the cyclone collector, and gas-solid separation is performed in the cyclone collector to collect ammonium sulfate particles;
preferably, the cyclone collector is a two-stage cyclone collector.
In the system for preparing ammonium sulfate from the active coke desulfurization rich gas, preferably, the tail gas treatment system comprises a tail gas absorption tower, a circulating pump is arranged outside the tail gas absorption tower, and an absorption liquid at the bottom of the tail gas absorption tower is conveyed to the top and continuously circulated;
preferably, the solution circulated by the circulating pump of the off-gas absorption tower is delivered to the reaction system.
In the system for preparing ammonium sulfate by using the active coke desulfurization rich gas as described above, preferably,
the solid content of the ammonium sulfate crystal slurry produced by the evaporation concentration system is 9-11%;
the water content of the ammonium sulfate produced by the dehydration drying system is less than 1 percent.
A method for preparing ammonium sulfate from active coke desulfurization rich gas specifically comprises the following steps:
the absorption reaction of the regeneration gas comprises the following steps:
reacting the regenerated gas subjected to desulfurization, denitrification and analysis by the activated coke with an absorption liquid to generate absorption slurry containing ammonium sulfate; preferably, the second step is carried out when the mass concentration of ammonium sulfate in the absorption slurry containing ammonium sulfate reaches 20-23%;
step two, the filtration, evaporation concentration and dehydration drying of the product comprise:
removing impurities from the absorption slurry containing ammonium sulfate to prepare a pure ammonium sulfate solution, and dehydrating, centrifugally separating and drying the pure ammonium sulfate solution after evaporation and concentration to obtain ammonium sulfate powder particles;
step three, tail gas treatment, comprising:
and (4) washing and purifying the tail gas generated in the processes of the first step and the second step by using an absorption liquid again, and emptying the treated gas.
In the method for preparing ammonium sulfate from the active coke desulfurization rich gas, preferably, the absorption liquid is ammonia water, and the mass concentration of the ammonia water is 18-20%;
still preferably, the method is performed using the system.
Compared with the closest prior art, the technical scheme provided by the invention has the following excellent effects:
the invention adopts a three-stage spraying device to fully absorb SO in the flue gas2Improving the utilization rate of the flue gas and increasing the generation rate of ammonium sulfate and SO2The loss rate is low.
The plate-and-frame filter press is arranged at the front end of the clarifier, so that the settling time of the clarifier and the equipment model selection of the clarifier are reduced, and the investment cost is reduced; a two-stage clarifier is used, carbon powder and impurities can be sufficiently removed, and the purity of ammonium sulfate is ensured to meet the quality requirement; the method can continuously produce ammonium sulfate powder products, is more suitable for continuous production requirements, and the nitrogen content of the obtained ammonium sulfate powder products is more than or equal to 21 percent, thereby meeting industrial use standards.
The cyclone and the centrifuge are adopted for dehydration, and the combination of the fluidized bed and the cyclone collector is used for drying, so that the water content of ammonium sulfate is greatly reduced, and the hardening problem of finished products is effectively avoided.
The secondary washing and absorption of the tail gas absorption tower ensure that the environment of a system workshop has no peculiar smell, and meanwhile, the treated gas can be directly discharged into the atmosphere and meets the emission standard; zero discharge of waste water is realized, the system has good circulation and no waste of water resources.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. Wherein:
FIG. 1 is a flow chart of a system for preparing ammonium sulfate from an activated coke desulfurization rich gas according to an embodiment of the invention.
In the figure: 1. a reaction system; 11. a reaction tower; 12. a spraying device; 121. a primary spray device; 122. a secondary spraying device; 123. a third stage spray device; 13. an oxidation fan; 14. an adjusting box; 2. a filtration system; 21. a plate-and-frame filter press; 22. a primary clarifier; 23. a secondary clarifier; 24. a buffer tank; 3. an evaporative concentration system; 31. a heater; 32. a separator; 33. an evaporation circulating pump; 34. a condenser; 35. a vacuum pump; 36. a vacuum tank; 4. a dehydration drying system; 41. a swirler; 42. a centrifugal device; 43. a fluidized bed; 44. a cyclone collector; 45. an induced draft fan; 5. a tail gas treatment system; 51. a tail gas absorption tower; 6. and a circulating pump.
Detailed Description
The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
In the description of the present invention, the terms "longitudinal", "lateral", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, which are for convenience of description of the present invention only and do not require that the present invention must be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. The terms "connected" and "connected" used herein should be interpreted broadly, and may include, for example, a fixed connection or a detachable connection; they may be directly connected or indirectly connected through intermediate members, and specific meanings of the above terms will be understood by those skilled in the art as appropriate.
As shown in fig. 1, according to an embodiment of the present invention, there is provided a system for preparing ammonium sulfate by recycling an activated coke desulfurization rich gas, the system for preparing ammonium sulfate includes:
reaction system 1 for absorbing SO in regeneration gas2After reaction, absorption slurry containing ammonium sulfate is generated;
the reaction system 1 includes: the reaction tower 11, the reaction tower 11 is used for regenerating SO in gas2Absorption of (i.e. absorption liquid and SO)2A reaction is carried out, a spraying device 12 is arranged in the reaction tower 11, the spraying device 12 is used for spraying absorption liquid, the ascending regeneration gas is fully contacted with the descending absorption liquid, mass transfer and absorption reaction are carried out, and ammonium sulfate is generated; the middle lower part of the reaction tower 11 is provided with a regeneration gas (i.e. active coke desulfurization rich gas) inlet, the inlet is positioned above the bottom absorption slurry, the outside of the reaction tower 11 is provided with an oxidation fan 13, a gas outlet of the oxidation fan 13 is connected with a slurry absorption pool in the reaction tower 11, and is used for oxidizing ammonium sulfite in the absorption slurry at the bottom of the reaction tower 11 (the absorption slurry can be pure absorption liquid at the beginning, and after the reaction tower 11 runs for a period of time, the absorption slurry contains ammonium sulfite, even ammonium sulfate) into ammonium sulfate; preferably, the reaction system 1 further includes a circulation pump 6, the circulation pump 6 is disposed outside the reaction tower 11, the circulation pump 6 circulates the absorption slurry at the bottom of the reaction tower 11 to the spray devices 12 disposed at the upper portion of the reaction tower 11, preferably, there are three spray devices 12, from bottom to top, which are respectively a first-stage spray device 121, a second-stage spray device 122 and a third-stage spray device 123, and the third-stage spray device 123 absorbs the regeneration gas layer by layer; correspondingly, 3 circulating pumps 6 are arranged, the absorption slurry at the bottom of the reaction tower 11 is respectively circulated to the corresponding first-stage spraying device 121, second-stage spraying device 122 and third-stage spraying device 123 so as to carry out three-stage spraying, most smoke dust and sulfur dioxide in the regeneration gas are removed by the first-stage spraying, the removal rate reaches 70%, the smoke gas continues to go upwards and then enters the second-stage spraying device 122, the removal rate of the smoke dust and the sulfur dioxide in the regeneration gas after the second-stage spraying can reach 80-85%, then the smoke gas goes upwards and enters the third-stage spraying device 123 arranged at the top of the tower so as to further remove the smoke dust and the sulfur dioxide, and the smoke dust and theThe removal rate reaches 88% -98%, and the purified tail gas (namely the gas discharged from the upper part of the absorption tower 11) enters a tail gas absorption system.
When the mass concentration of ammonium sulfate in the absorption slurry at the bottom of the reaction tower 11 reaches 20-23% (e.g. 20.5%, 21%, 21.5%, 22%, 22.5%, 23%), the absorption slurry is discharged into the filtering system 2 at the next stage.
In an embodiment of the present invention, the absorption liquid is ammonia water, and the mass concentration of the ammonia water is 18-20% (e.g., 18.2%, 18.4%, 18.6%, 18.8%, 19%, 19.2%, 19.4%, 19.6%, 19.8%, 20%).
The filtering system 2 is connected with a slurry outlet of the reaction system 1 and is used for removing carbon powder and impurities in the slurry to obtain a purified ammonium sulfate solution;
preferably, a regulating box 14 is arranged between the reaction system 1 and the filtering system 2, and slurry from the reaction system 1 enters the regulating box 14 for buffering and then enters the filtering system 2; the slurry in the reaction system 1 is periodically discharged into the conditioning tank 14 according to actual production conditions, and the water quality and the water amount are adjusted in the conditioning tank 14. Because the components and the contents of the flue gas entering the reaction tower 11 are not completely the same, the components of the absorption slurry containing ammonium sulfate at the bottom of the reaction tower 11 are different, the slurry is firstly discharged into the regulating box 14 for storage, and is discharged into the next-stage filtering system 2 in a timed and quantitative manner after being stored for a certain amount, so that the components of the slurry in the regulating box 14 are as uniform as possible, the subsequent system can stably operate, the components and the slurry amount of the slurry can be discharged into the filtering system 2 as uniform as possible, and the stability and the continuity of the system are ensured.
The filtering system 2 comprises a plate-and-frame filter press 21 and a clarifier; the inlet of the plate-and-frame filter press 21 is connected with the slurry outlet of the reaction system 1, and the inlet of the clarifier is connected with the slurry outlet of the plate-and-frame filter press 21; returning the sediment at the bottom of the clarifier to the plate-and-frame filter press 21 again for filtration; and (3) filtering the slurry discharged from the reaction system 1 in a plate-and-frame filter press 21, and settling and purifying the slurry flowing out of the plate-and-frame filter press 21 in a clarifier to obtain a pure ammonium sulfate solution.
In the embodiment of the invention, the clarifier comprises two stages, namely a primary clarifier 22 and a secondary clarifier 23, wherein an overflow port of the primary clarifier 22 is connected with an inlet of the secondary clarifier 23, and precipitates at the bottoms of the primary clarifier 22 and the secondary clarifier 23 are returned to the plate-and-frame filter press 21 for further filtration to recover ammonium sulfate.
Still preferably, the filtration system 2 further comprises a buffer tank 24, and the overflow liquid of the secondary clarifier 23 enters the buffer tank 24 and then enters the evaporation concentration system 3 at the lower stage.
Preferably, the vacuum pump 35 is connected to the vacuum tank 36, the vacuum tank 36 plays a role of buffering, the vacuum tank 36 is vacuumized by the vacuum pump 35, the top outlet of the condenser 34 is connected to the vacuum tank 36 to make the inside of the condenser 34 be in a negative pressure environment, and the water condensed and cooled in the condenser 34 is conveyed to the vacuum tank 36 through the bottom outlet to complete the cooling and recovery process of the steam.
Preferably, the ammonium sulfate slurry in the separator 32 enters the dewatering and drying system 4 when the solid content reaches 9-11%. The slurry in the heater 31 is evaporated and concentrated at a temperature of 80-100 ℃.
And the dehydration drying system 4 is used for dehydrating and drying the ammonium sulfate crystal slurry to form an ammonium sulfate powder finished product. The dewatering and drying system 4 includes a cyclone 41, a centrifugal device 42 and a drying device.
The inlet of the cyclone 41 is connected with the concentrated slurry outlet of the separator 32 and is used for solid-liquid separation and dehydration of the ammonium sulfate slurry; the bottom slurry outlet of the cyclone 41 is connected with the inlet of the centrifugal device 42 and is used for further dehydration and recovery of solid materials containing ammonium sulfate; the drying means is connected to the solids outlet of the centrifugal means 42 for drying the solid material containing ammonium sulphate. The solid content of the ammonium sulfate slurry at the lower outlet after the dehydration of the cyclone 41 is 30-40%. The solid ammonium sulfate separated from the centrifugal device 42 has a water content of about 3 to 5% and is then sent to a drying device. The centrifugal device 42 comprises a centrifugal separator and a cover body, the centrifugal separator is arranged in the cover body, and filter cakes after centrifugal separation enter the drying device through a chute.
The drying device comprises a fluidized bed 43 and a cyclone collector 44, solid ammonium sulfate discharged from the centrifugal device 42 enters the fluidized bed 43 for drying, the fluidized bed 43 is provided with a heating device, a drying heat source is hot air, and the solid ammonium sulfate is dried to reduce the water content to below 1% so as to avoid hardening during storage. The gas outlet of the fluidized bed 43 and the gas outlet of the centrifugal device 42 are both connected to the inlet of the cyclone collector 44, and gas-solid separation is performed in the cyclone collector 44 to collect ammonium sulfate powder particles. Preferably, the cyclone collector 44 is a two-stage cyclone collector 44.
Preferably, during the drying process, the upper liquid outlet of the cyclone 41 and the supernatant outlet of the centrifugal device 42 are both connected to the reaction system 1, and the mixture is sent to the reaction tower 11 due to the small ammonium sulfate content, and then further absorption reaction is performed, so that the mixture can be used as the circulating slurry of the absorption tower 11.
The ammonium sulfate produced by the fluidized bed 43 is finished ammonium sulfate powder, white crystals and the nitrogen content (calculated by dry basis) is more than or equal to 21 percent.
And the tail gas treatment system 5 is connected with the tail gas outlets of the dehydration drying system 4 and the reaction system 1 respectively, and is used for purifying and treating tail gas generated by the dehydration drying system 4 and the reaction system 1. Preferably, the tail gas of the dehydration drying system 4 enters the tail gas treatment system 5 after being pressurized by the induced draft fan 45; specifically, the tail gas outlet of the cyclone collector 44 is pressurized by the induced draft fan 45 and then conveyed into the tail gas absorption tower 51 for purification treatment.
The tail gas treatment system 5 comprises a tail gas absorption tower 51, a circulating pump 6 is arranged outside the tail gas absorption tower 51, and the absorption liquid at the bottom of the tail gas absorption tower 51 is conveyed to the top and continuously circulated so as to further absorb sulfur dioxide and dust in the tail gas. The bottom of the tail gas absorption tower 51 is provided with an absorption liquid pool, residual tail gas enters from the lower part of the tail gas absorption tower 51, an inlet of the residual tail gas is arranged above the absorption liquid pool at the bottom of the tail gas absorption tower 51, a circulating pump 6 arranged outside the tail gas absorption tower 51 conveys the absorption liquid at the bottom of the tail gas absorption tower 51 to the top for spraying, the absorption liquid continuously circulates, and the sprayed absorption liquid is contacted with the tail gas which goes upwards. When the concentration of the continuously circulated absorption liquid reaches a certain value, the absorption liquid is periodically conveyed to the reaction system 1 so as to be absorbed and utilized again. The gas purified and treated by the tail gas absorption tower 51 is discharged to the air at high altitude, so as to reach the atmospheric emission standard. The absorption liquid in the absorption liquid pool at the bottom of the off-gas absorption tower 51 is an ammonia water solution, and preferably an ammonia water solution with a mass concentration of 18-20% (e.g., 18.2%, 18.4%, 18.6%, 18.8%, 19%, 19.2%, 19.4%, 19.6%, 19.8%, 20%) is used.
In order to further understand the system for preparing ammonium sulfate from the active coke desulfurization rich gas, the invention also provides a method for preparing ammonium sulfate from the active coke desulfurization rich gas, which comprises the following steps:
the absorption reaction of the regeneration gas comprises the following steps:
the regenerated gas after desulfurization and denitrification analysis of the activated coke is sprayed by the first-to-third-stage spraying devices of the reaction system 1 and absorbed by the absorption liquid to generate absorption slurry containing ammonium sulfate, and when the mass concentration of the ammonium sulfate in the slurry reaches 20-23% (such as 20.5%, 21%, 21.5%, 22%, 22.5% and 23%), the slurry is discharged to be filtered in the next step.
Step two, the filtration, evaporation concentration and dehydration drying of the product comprise:
the absorption slurry containing ammonium sulfate enters the regulating box 14, carbon powder and impurities are removed through the filtration of the plate-and-frame filter press 21, then the absorption slurry enters the primary clarifier 22 and the secondary clarifier 23 in sequence for precipitation and purification, a purified ammonium sulfate solution obtained from an overflow outlet of the secondary clarifier 23 enters the buffer tank 24, and the precipitated precipitate enters the plate-and-frame filter press 21 again for filtration; the liquid in the buffer tank 24 enters an evaporation concentration system 3, ammonium sulfate crystal slurry is obtained after evaporation concentration, then the slurry is dehydrated in two stages through a cyclone 41 and a centrifugal device 42 to obtain an ammonium sulfate solid material with low water content, the material is sent into a fluidized bed 43 to be dried to obtain finished ammonium sulfate particles, and tail gas of the fluidized bed 43 and the centrifugal device 42 is collected through a two-stage cyclone collector 44 to obtain finished ammonium sulfate particles; the upper liquid outlet of the cyclone 41 and the supernatant outlet of the centrifugal device 42 are sent to the reaction tower 11 for further absorption reaction.
Step three, tail gas treatment, comprising:
tail gas generated by the reaction tower 11 and the cyclone collector 44 enters the tail gas absorption tower 51, ammonia water solution is adopted for washing and purifying, the ammonia water solution in the tail gas absorption tower 51 is continuously and circularly sprayed from bottom to top, and the circulating absorption liquid is periodically conveyed to the reaction tower 11 for reaction after the concentration of the circulating absorption liquid reaches a certain numerical value, so that the resource utilization is maximized, and the treated gas is emptied at high altitude after being purified.
In summary, the inventionThe system and the method for preparing ammonium sulfate by recycling the active coke desulfurization rich gas have the following excellent effects: fully absorbing SO in flue gas by adopting three-stage spraying device2Improving the utilization rate of the flue gas and increasing the generation rate of ammonium sulfate and SO2The loss rate is low.
The plate-and-frame filter press is arranged at the front end of the clarifier, so that the settling time of the clarifier and the equipment model selection of the clarifier are reduced, and the investment cost is reduced; a two-stage clarifier is used, carbon powder and impurities can be sufficiently removed, and the purity of ammonium sulfate is ensured to meet the quality requirement; the method can continuously produce ammonium sulfate powder products, is more suitable for continuous production requirements, and the nitrogen content of the obtained ammonium sulfate powder products is more than or equal to 21 percent, thereby meeting industrial use standards.
The cyclone and the centrifuge are adopted for dehydration, and the combination of the fluidized bed and the cyclone collector is used for drying, so that the water content of the ammonium sulfate is greatly reduced, and the hardening problem of finished products is effectively avoided.
The secondary washing and absorption of the tail gas absorption tower ensure that the environment of a system workshop has no peculiar smell, and the treated gas can be directly discharged into the atmosphere and meets the emission standard; zero discharge of waste water is realized, the system has good circulation and no waste of water resources.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A system for preparing ammonium sulfate from active coke desulfurization rich gas is characterized by comprising:
reaction system for absorbing SO in the regeneration gas2After reaction, absorption slurry containing ammonium sulfate is generated;
the filtering system is connected with a slurry outlet of the reaction system and is used for removing carbon powder and impurities in the slurry to obtain a purified ammonium sulfate solution;
the solution outlet of the filtering system is connected with the inlet of the evaporation concentration system, and the evaporation concentration system is used for carrying out evaporation concentration on the purified ammonium sulfate solution to form ammonium sulfate crystal slurry;
the outlet of the evaporation concentration system is connected with the inlet of the desulfurization drying system, and the dehydration drying system is used for dehydrating and drying the ammonium sulfate crystal slurry to form an ammonium sulfate powder finished product;
and the tail gas treatment system is respectively connected with the dehydration drying system and the tail gas outlet of the reaction system and is used for purifying and treating tail gas generated by the dehydration drying system and the reaction system.
2. The system for preparing ammonium sulfate by using the active coke desulfurization rich gas as claimed in claim 1, wherein the reaction system comprises: reaction column for regenerating SO in a gas2The reaction tower is internally provided with a spraying device which is used for spraying absorption slurry, and the ascending regeneration gas and the descending absorption slurry are contacted and reacted to generate ammonium sulfate; an oxidation fan is arranged outside the reaction tower, and a gas outlet of the oxidation fan is connected with an absorption slurry pool at the bottom of the reaction tower and used for oxidizing ammonium sulfite in the absorption slurry into ammonium sulfate;
preferably, the reaction system further comprises a circulating pump, the circulating pump is arranged outside the reaction tower, and the circulating pump circulates the absorption slurry at the bottom of the reaction tower to the upper part of the reaction tower for spraying;
preferably, the spraying devices are multiple, and the multiple spraying devices absorb the regeneration gas layer by layer; the number of the spraying devices is preferably three;
still preferably, the absorption slurry containing ammonium sulfate enters the filtration system when the mass concentration of ammonium sulfate in the absorption slurry containing ammonium sulfate at the bottom of the reaction tower is 20-23%.
3. The system for preparing ammonium sulfate by using the active coke desulfurization rich gas as claimed in claim 1 or 2, wherein the filtering system comprises a plate-and-frame filter press and a clarifier; the inlet of the plate-and-frame filter press is connected with the slurry outlet of the reaction system, and the inlet of the clarifier is connected with the slurry outlet of the plate-and-frame filter press; returning the sediment at the bottom of the clarifier to the plate-and-frame filter press again for filtering, feeding the absorption slurry containing ammonium sulfate of the reaction system into the plate-and-frame filter press for filtering, feeding the slurry flowing out of the plate-and-frame filter press into the clarifier for precipitation and purification, and obtaining a pure ammonium sulfate solution;
preferably, the clarifier comprises two stages, namely a first-stage clarifier and a second-stage clarifier, wherein an overflow port of the first-stage clarifier is connected with an inlet of the second-stage clarifier;
preferably, a regulating box is arranged between the reaction system and the filtering system, and slurry from the reaction system enters the regulating box firstly and then enters the filtering system;
still preferably, the filtration system further comprises a buffer tank into which overflow liquid of the secondary clarifier enters.
4. The system for preparing ammonium sulfate by using the active coke desulfurization rich gas as claimed in claim 3, wherein the evaporation concentration system comprises:
the heater comprises a tube pass and a shell pass, the tube pass is used for storing slurry, the shell pass is used for storing hot steam, and the heater is connected with a slurry outlet of the buffer tank and is used for heating, evaporating and concentrating an ammonium sulfate solution to form ammonium sulfate crystal slurry;
the inlet of the separator is connected with the tube pass outlet of the heater, the separator is used for carrying out gas-liquid separation on the ammonium sulfate crystal slurry, and the bottom circulating slurry outlet of the separator is connected to the tube pass bottom inlet of the heater through an evaporation circulating pump, so that the slurry is continuously circulated and evaporated; the bottom concentrated slurry outlet of the separator is connected with the dehydration drying system;
the condenser is used for cooling the steam from the separator and the heater;
the vacuum pump is connected with the condenser and enables negative pressure to be formed in the condenser; preferably also creating a negative pressure within the separator;
preferably, the vacuum pump is connected to the vacuum tank, and both a top outlet and a bottom outlet of the condenser are connected to the vacuum tank.
5. The system for preparing ammonium sulfate by using the active coke desulfurization rich gas as claimed in claim 1, wherein the dehydration drying system comprises a cyclone, a centrifugal device and a drying device;
the inlet of the cyclone is connected with the slurry outlet of the evaporation concentration system and is used for carrying out solid-liquid separation and dehydration on the ammonium sulfate slurry; a bottom slurry outlet of the cyclone is connected with an inlet of the centrifugal device for further dehydration, and a solid material containing the ammonium sulfate is recovered; the drying device is connected with a solid outlet of the centrifugal device and is used for drying the solid material containing the ammonium sulfate;
preferably, the upper liquid outlet of the cyclone and the supernatant outlet of the centrifuge are both connected to the reaction system.
6. The system for preparing ammonium sulfate by using the active coke desulfurization rich gas as claimed in claim 5, wherein the drying device comprises a fluidized bed and a cyclone collector, a gas outlet of the fluidized bed and a gas outlet of the centrifugal device are both connected with an inlet of the cyclone collector, and gas-solid separation is carried out in the cyclone collector to collect ammonium sulfate particles;
preferably, the cyclone collector is a two-stage cyclone collector.
7. The system for preparing ammonium sulfate from active coke desulfurization rich gas as claimed in claim 1, wherein the tail gas treatment system comprises a tail gas absorption tower, a circulating pump is arranged outside the tail gas absorption tower, and the absorption liquid at the bottom of the tail gas absorption tower is conveyed to the top and continuously circulated;
preferably, the solution circulated by the circulating pump of the off-gas absorption tower is delivered to the reaction system.
8. The system for preparing ammonium sulfate by using the active coke desulfurization rich gas as claimed in claim 1,
the solid content of the ammonium sulfate crystal slurry produced by the evaporation concentration system is 9-11%;
the water content of the ammonium sulfate produced by the dehydration drying system is less than 1 percent.
9. A method for preparing ammonium sulfate from active coke desulfurization rich gas is characterized by comprising the following steps:
the absorption reaction of the regeneration gas comprises the following steps:
reacting the regenerated gas subjected to desulfurization, denitrification and analysis by the activated coke with an absorption liquid to generate absorption slurry containing ammonium sulfate; preferably, the second step is carried out when the mass concentration of ammonium sulfate in the absorption slurry containing ammonium sulfate reaches 20-23%;
step two, the filtration, evaporation concentration and dehydration drying of the product comprise:
removing impurities from the absorption slurry containing ammonium sulfate to prepare a pure ammonium sulfate solution, and dehydrating, centrifugally separating and drying the pure ammonium sulfate solution after evaporation and concentration to obtain ammonium sulfate powder particles;
step three, tail gas treatment, comprising:
and (4) washing and purifying the tail gas generated in the processes of the first step and the second step by using an absorption liquid again, and emptying the treated gas.
10. The method for preparing ammonium sulfate from the active coke desulfurization rich gas as claimed in claim 9, wherein the absorption liquid is ammonia water, and the mass concentration of the ammonia water is 18-20%;
still preferably, the method is performed using the system of any one of claims 1-8.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113213509A (en) * | 2021-04-26 | 2021-08-06 | 聊城市鲁西化工工程设计有限责任公司 | Ammonium sulfate solution concentration drying system, process and application |
| CN117942875A (en) * | 2024-03-27 | 2024-04-30 | 山东天力能源股份有限公司 | Liquid crystal polymer solid phase polycondensation reaction device and reaction method thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11347405A (en) * | 1998-06-10 | 1999-12-21 | Tetsugen Corp | Reusing method of activated coke |
| CN101549246A (en) * | 2009-04-30 | 2009-10-07 | 杭州三和环保技术工程有限公司 | Sintering flue gas desulfurization combined coking coal gas deamination cycling technology and cycling system |
| CN101757848A (en) * | 2009-12-17 | 2010-06-30 | 北京博奇电力科技有限公司 | Process and device for processing smoke containing sulfur dioxide and preparing solid ammonium sulfate |
| CN105771611A (en) * | 2016-01-27 | 2016-07-20 | 西安航天源动力工程有限公司 | Graded tower internal crystallization ammonia-process desulfurization system |
| CN110316896A (en) * | 2019-08-13 | 2019-10-11 | 北京中航泰达环保科技股份有限公司 | Dry reactive coke/charcoal desulphurization denitration rich gas pretreated waste water processing system |
-
2020
- 2020-01-21 CN CN202010072076.0A patent/CN111153416A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11347405A (en) * | 1998-06-10 | 1999-12-21 | Tetsugen Corp | Reusing method of activated coke |
| CN101549246A (en) * | 2009-04-30 | 2009-10-07 | 杭州三和环保技术工程有限公司 | Sintering flue gas desulfurization combined coking coal gas deamination cycling technology and cycling system |
| CN101757848A (en) * | 2009-12-17 | 2010-06-30 | 北京博奇电力科技有限公司 | Process and device for processing smoke containing sulfur dioxide and preparing solid ammonium sulfate |
| CN105771611A (en) * | 2016-01-27 | 2016-07-20 | 西安航天源动力工程有限公司 | Graded tower internal crystallization ammonia-process desulfurization system |
| CN110316896A (en) * | 2019-08-13 | 2019-10-11 | 北京中航泰达环保科技股份有限公司 | Dry reactive coke/charcoal desulphurization denitration rich gas pretreated waste water processing system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113213509A (en) * | 2021-04-26 | 2021-08-06 | 聊城市鲁西化工工程设计有限责任公司 | Ammonium sulfate solution concentration drying system, process and application |
| CN117942875A (en) * | 2024-03-27 | 2024-04-30 | 山东天力能源股份有限公司 | Liquid crystal polymer solid phase polycondensation reaction device and reaction method thereof |
| CN117942875B (en) * | 2024-03-27 | 2024-06-21 | 山东天力能源股份有限公司 | Liquid crystal polymer solid phase polycondensation reaction device and reaction method thereof |
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Application publication date: 20200515 |