CN111170339B - System and method for preparing sodium sulfite by recycling active coke desulfurization rich gas - Google Patents
System and method for preparing sodium sulfite by recycling active coke desulfurization rich gas Download PDFInfo
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- CN111170339B CN111170339B CN202010072611.2A CN202010072611A CN111170339B CN 111170339 B CN111170339 B CN 111170339B CN 202010072611 A CN202010072611 A CN 202010072611A CN 111170339 B CN111170339 B CN 111170339B
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- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 title claims abstract description 153
- 235000010265 sodium sulphite Nutrition 0.000 title claims abstract description 76
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 42
- 230000023556 desulfurization Effects 0.000 title claims abstract description 40
- 238000004064 recycling Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000000571 coke Substances 0.000 title claims description 45
- 238000006243 chemical reaction Methods 0.000 claims abstract description 79
- 239000002002 slurry Substances 0.000 claims abstract description 70
- 238000011084 recovery Methods 0.000 claims abstract description 44
- 238000001704 evaporation Methods 0.000 claims abstract description 37
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000010521 absorption reaction Methods 0.000 claims abstract description 36
- 238000011282 treatment Methods 0.000 claims abstract description 31
- 230000008020 evaporation Effects 0.000 claims abstract description 28
- 239000000428 dust Substances 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 21
- 238000001816 cooling Methods 0.000 claims abstract description 20
- 230000008929 regeneration Effects 0.000 claims abstract description 19
- 238000011069 regeneration method Methods 0.000 claims abstract description 19
- 230000002194 synthesizing effect Effects 0.000 claims abstract description 11
- 239000007787 solid Substances 0.000 claims abstract description 10
- 238000000746 purification Methods 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 225
- 239000007788 liquid Substances 0.000 claims description 73
- 238000005406 washing Methods 0.000 claims description 54
- 239000003513 alkali Substances 0.000 claims description 38
- 238000001035 drying Methods 0.000 claims description 30
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 22
- 239000012452 mother liquor Substances 0.000 claims description 19
- 239000000843 powder Substances 0.000 claims description 10
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 10
- 238000011049 filling Methods 0.000 claims description 9
- 238000005201 scrubbing Methods 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 6
- 238000012546 transfer Methods 0.000 claims description 5
- 238000004458 analytical method Methods 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 4
- 239000011343 solid material Substances 0.000 claims description 4
- 239000000725 suspension Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000006194 liquid suspension Substances 0.000 claims description 3
- 230000001052 transient effect Effects 0.000 claims description 3
- 239000000112 cooling gas Substances 0.000 claims description 2
- -1 polytetrafluoroethylene Polymers 0.000 claims description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 6
- 238000010924 continuous production Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 23
- 239000003546 flue gas Substances 0.000 description 23
- 239000000047 product Substances 0.000 description 11
- 235000017550 sodium carbonate Nutrition 0.000 description 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 8
- 239000012535 impurity Substances 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 238000005245 sintering Methods 0.000 description 5
- 239000000945 filler Substances 0.000 description 4
- 239000012065 filter cake Substances 0.000 description 4
- 238000012856 packing Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Substances [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 238000001802 infusion Methods 0.000 description 3
- 230000010354 integration Effects 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- AHEWZZJEDQVLOP-UHFFFAOYSA-N monobromobimane Chemical compound BrCC1=C(C)C(=O)N2N1C(C)=C(C)C2=O AHEWZZJEDQVLOP-UHFFFAOYSA-N 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/14—Preparation of sulfites
-
- 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
- B01D53/02—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 by adsorption, e.g. preparative gas chromatography
-
- 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
-
- 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model provides a system and a method for preparing sodium sulfite by recycling active desulfurization rich gas, wherein the system comprises the following steps: the pretreatment system is used for purifying, cooling and gas-solid separation of the regenerated gas; the reaction recovery system comprises a reaction unit and a recovery unit, and the reaction unit of the reaction recovery system is connected with a gas outlet of the pretreatment system and is used for synthesizing and recovering sodium sulfite in a reaction manner; the evaporation concentration system is used for circularly evaporating and concentrating the sodium sulfite slurry generated by the reaction unit, and the sodium sulfite slurry subjected to evaporation concentration enters from the inlet of the recovery unit so as to be recovered; and the tail gas treatment system is used for absorbing sulfur dioxide and dust in the tail gas. The method comprises the following steps: pretreatment of the regeneration gas; synthesizing, evaporating, concentrating and recycling a product; and (5) tail gas treatment. The system of the utility model has low energy consumption, high purity, good absorption and purification effect, less water consumption and SO, and is suitable for continuous production requirements 2 The loss rate is low, and the system independence is strong.
Description
Technical Field
The utility model belongs to the technical field of dry active coke desulfurization and denitrification rich gas recycling in the environment-friendly industry, and particularly relates to a system and a method for preparing sodium sulfite by recycling active coke desulfurization rich gas.
Background
Currently, the treatment measures of atmospheric pollutants for iron and steel enterprises in China can be summarized into three main categories: 1. raw material control and flue gas emission reduction basic conditions; 2. an effective means of controlling the sintering process and reducing the emission of flue gas; 3. and (3) treating the tail end of the flue gas, and finally ensuring the final means of the flue gas treatment. Among the above three treatments, one tends to pay more attention to the end treatment of flue gas. At present, the treatment of the tail end of the sintering flue gas mainly comprises the technologies of active coke desulfurization and denitration integration, flue gas desulfurization (wet method, dry method and semi-dry method) +medium-low temperature SCR denitration integration and the like.
Flue gas desulfurization (wet method, dry method and semi-dry method) +medium-low temperature SCR denitration integration is generally that the tail end of sintering flue gas is treated by flue gas treatment system, and harmful substance SO in the flue gas is removed by absorption 2 And NOx, and substances after tail gas absorption treatment cannot be recycled; the dry active coke desulfurizing and denitrating technology uses active coke to treat SO in fume 2 And 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, and 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:
the regenerated gas generated by the dry active coke desulfurization and denitrification technology contains more SO 2 The gas is absorbed and analyzed by active coke to obtain high-concentration SO 2 Gas, if SO with high concentration 2 The gas is reasonably utilized and used as an industrial preparation raw material to prepare industrial sodium sulfite salt, and the sintering flue gas is recycled, so that the environmental pollution is reduced, and the method has important significance for improving the industrial production process.
Accordingly, there is a need to provide an improved solution to the above-mentioned deficiencies of the prior art.
Disclosure of Invention
The utility model aims to provide a system and a method for preparing sodium sulfite by recycling active coke desulfurization rich gas, which are used for solving the problems that the utilization rate of sintering flue gas is low, polluted flue gas cannot be recycled and resource waste is caused in the existing steel production process.
In order to achieve the above object, the present utility model provides the following technical solutions:
a system for producing sodium sulfite by active coke desulfurization rich gas recycling, the system comprising:
the pretreatment system is used for purifying, cooling and gas-solid separation of the regenerated gas to obtain pretreated gas with higher sulfur dioxide purity;
the reaction recovery system comprises a reaction unit and a recovery unit, and the reaction unit of the reaction recovery system is connected with a gas outlet of the pretreatment system and is used for synthesizing and recovering sodium sulfite in a reaction manner;
the evaporation concentration system is connected with the outlet of the reaction unit and is used for circularly evaporating and concentrating sodium sulfite slurry generated by the reaction unit, and the sodium sulfite slurry subjected to evaporation concentration enters from the inlet of the recovery unit of the reaction recovery system so as to be recovered;
and the tail gas treatment system is connected with a tail gas outlet of the reaction recovery system and is used for purifying the tail gas generated in the reaction recovery system so as to further absorb sulfur dioxide and dust in the tail gas.
In the system for preparing sodium sulfite by recycling active coke desulfurization rich gas as described above, preferably, the pretreatment system comprises: scrubber for purifying gas to remove SO in regeneration gas 3 HCl, HF and dust, and simultaneously realizing gas cooling and gas-liquid separation;
preferably, the scrubber comprises two stages of scrubbers connected in sequence, wherein the first stage of scrubber is used for purifying active coke regeneration gas to primarily remove SO therein 3 HCl, HF and dust and preliminarily realizing gas cooling; two-stage scrubber for re-useSecondary purifying the gas from said primary scrubber to further remove SO therefrom 3 HCl, HF and dust, further realizing gas cooling, and simultaneously removing fog drops in the gas after the secondary purification;
more preferably, a vortex generating device is arranged at the upper part of the inner part of the primary scrubber, a washing circulating pump is arranged at the outer part of the primary scrubber, and washing liquid at the bottom of the primary scrubber enters the vortex generating device through the washing circulating pump to generate a transient vortex liquid suspension layer and then forms a downward running rotating liquid flow to perform an impact reaction with the upward regeneration gas;
further preferably, the vortex generating device is provided with an upper layer and a lower layer which are respectively a first vortex generating device and a second vortex generating device;
further preferably, the secondary scrubber comprises a scrubbing section, a packing section and an electric defogging section from bottom to top;
further preferably, a washing circulating pump and a cooler are arranged outside the washing section and are used for circulating washing liquid and cooling gas of the washing section respectively;
still preferably, the gas dust and total salt content passing through the secondary scrubber is less than 5mg/m 3 。
In the system for preparing sodium sulfite by recycling active coke desulfurization rich gas as described above, preferably, the reaction unit of the reaction recovery system comprises:
the reaction device is connected with a gas outlet of the pretreatment system and is used for synthesizing sodium sulfite by reaction;
the recovery unit includes: the centrifugal device is connected with a concentrated slurry outlet of the evaporation concentration system and is used for recovering solid materials containing the sodium sulfite; the drying device is connected with the solid outlet of the centrifugal device and is used for drying the solid material containing the sodium sulfite;
the reaction device comprises a first-stage reactor and a second-stage reactor, wherein the pretreated gas enters the first-stage reactor, and an upper gas outlet of the first-stage reactor is connected to an upper gas inlet of the second-stage reactor through a first gas pipeline; the first gas pipeline is used for conveying gas containing sulfur dioxide; the bottom slurry outlet of the primary reactor is connected to the evaporation concentration system through a pipeline; the lower slurry outlet of the secondary reactor is connected to the upper slurry inlet of the primary reactor through a first infusion pipeline, and the first infusion pipeline is used for conveying slurry;
preferably, the secondary reactor is connected with an alkali liquor tank, and alkali liquor in the alkali liquor tank is periodically conveyed to be supplemented into the secondary reactor;
still preferably, the secondary reactor is provided with a circulation pump for self-circulation of the slurry.
In the system for preparing sodium sulfite by recycling active coke desulfurization rich gas as described above, preferably, the evaporation concentration system comprises:
the heater comprises a tube side and a shell side, wherein the tube side is used for storing slurry, the shell side is used for storing hot steam, and the heater is connected with a bottom slurry outlet of the primary reactor and is used for heating, evaporating and concentrating sodium sulfite slurry;
the inlet of the separator is connected with the tube side outlet of the heater, the separator is used for carrying out gas-liquid separation on the sodium sulfite slurry, and the bottom circulating slurry outlet of the separator conveys the slurry to the tube side bottom inlet of the heater through an evaporation circulating pump so as to continuously and circularly evaporate the slurry; the bottom concentrated slurry outlet of the separator is connected with the centrifugal device;
the upper steam outlet of the separator and the shell side upper steam outlet of the heater are connected with the condenser, and the condenser is used for cooling the steam from the separator and the heater;
the vacuum pump is connected with the condenser to form negative pressure in the condenser; preferably, a negative pressure is also created in the separator;
preferably, the vacuum pump is connected to the vacuum tank, and both the top outlet and the bottom outlet of the condenser are connected to the vacuum tank.
In the system for preparing sodium sulfite by recycling active coke desulfurization rich gas as described above, preferably, the reaction unit further comprises a mother liquor tank, the liquid generated by the centrifugal device and the tail gas treatment system is conveyed into the mother liquor tank, and the liquid in the mother liquor tank is conveyed into the alkali liquor tank through a pipeline.
In the system for preparing sodium sulfite by recycling the active coke desulfurization rich gas as described above, preferably, the drying device comprises an air dryer and a cyclone collector, and the material dried by the air dryer enters the cyclone collector for particle collection;
preferably, the cyclone collector is a two-stage cyclone collector.
In the system for preparing sodium sulfite by recycling active coke desulfurization rich gas, preferably, a drying feeder is further arranged before the air dryer, and materials enter a drying space in the drying feeder and are transported to the air dryer.
In the system for preparing sodium sulfite by recycling active coke desulfurization rich gas as described above, preferably, the tail gas treatment system comprises a tail gas absorption tower, and a circulating pump is arranged outside the tail gas absorption tower, so that alkali liquor at the bottom of the tail gas absorption tower is conveyed to the top and continuously circulated.
The method for preparing sodium sulfite by recycling active coke desulfurization rich gas specifically comprises the following steps:
step one, pretreatment of regeneration gas, comprising:
purifying the regenerated gas after desulfurization, denitrification and analysis of the active coke by a pretreatment system to obtain pretreated gas with high sulfur dioxide purity;
step two, synthesizing, evaporating, concentrating and recycling the product, comprising the following steps:
the pretreated gas enters a reaction unit of a reaction recovery system, sodium sulfite slurry is prepared by adopting absorption liquid through a two-stage reaction device, and then the sodium sulfite slurry is subjected to evaporation concentration and then centrifugal separation and drying by the recovery unit to obtain sodium sulfite powder particles;
step three, tail gas treatment, which comprises the following steps:
and the tail gas generated by the reaction unit and the recovery unit enters the tail gas treatment system, absorption liquid is adopted for washing and purifying again, and the treated gas is exhausted.
In the method for preparing sodium sulfite by recycling the active coke desulfurization rich gas as described above, preferably, the pretreated gas enters a reaction unit of the reaction recovery system after being pressurized by a tail gas fan;
preferably, the absorption liquid is alkali liquor, more preferably sodium carbonate solution;
still preferably, the method is accomplished using the system.
Compared with the closest prior art, the technical scheme provided by the utility model has the following excellent effects:
the system and the method for preparing the sodium sulfite by recycling the active coke desulfurization rich gas have the following excellent effects:
the primary reactor and the secondary reactor are communicated and shared, SO that the reaction time of the primary reactor can be stabilized, the influence on the discharge of the primary reactor caused by the failure of the reactor is reduced, the continuous and stable operation of a downstream evaporation concentration system, a centrifugal separation system and a drying system is facilitated, and the SO absorbed by the primary reactor is increased 2 The concentration of the alkali liquor is reduced, and the method is beneficial to the reduction of the energy consumption of the system and the improvement of the product quality.
The sodium sulfite powder product can be continuously produced, the continuous production requirement is met, the purity of the obtained sodium sulfite powder product is more than 90 percent, and the industrial use standard is met.
The two-stage vortex generating device is adopted to generate circulating rotary liquid flow to continuously wash the flue gas, SO that better absorption and purification effects can be achieved, the water consumption is low, and SO (SO) 2 The loss rate is lower.
The absolute circulation quantity of the circulating absorption liquid is effectively reduced by adopting a two-stage absorption method, and simultaneously SO in the waste gas is improved 2 Is SO using the method and system of the present utility model 2 The absorptivity is more than 98%, the alkali liquor consumption is less, and the treated gas can be directly discharged into the atmosphere to meet the emission standard.
The pretreatment system is relatively independent and has no related interlocking relation with the later reaction recovery system, and when the pretreatment system fails, the pretreatment system can be directly replaced by a standby device, so that the influence on a downstream sodium sulfite powder product preparation system is reduced.
Drawings
The accompanying drawings, which are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate embodiments of the utility model and together with the description serve to explain the utility model. Wherein:
FIG. 1 is a flow chart of a system for preparing sodium sulfite by recycling active coke desulfurization rich gas in an embodiment of the utility model.
In the figure: 1. a pretreatment system; 11. a primary scrubber; 111. a first vortex generating device; 112. a second vortex generating device; 12. a secondary scrubber; 121. a washing section; 122. a filler section; 123. an electric defogging section; 13. a washing circulation pump; 14. a cooler; 15. a wastewater tank; 2. a reaction recovery system; 21. a first stage reactor; 22. a secondary reactor; 23. an alkali solution tank; 24. a mother liquor tank; 25. a centrifuge; 26. a drying feeder; 27. an air dryer; 28. a cyclone collector; 29. a tail gas fan; 210. an induced draft fan; 211. a first gas transmission pipeline; 212. a first infusion line; 3. an evaporation concentration system; 31. a heater; 32. a separator; 33. an evaporation circulation pump; 34. a condenser; 35. a vacuum pump; 36. a vacuum tank; 4. a tail gas treatment system; 41. a tail gas absorption tower; 5. and a circulation pump.
Detailed Description
The utility model will be described in detail below with reference to the drawings in connection with embodiments. It should be noted that, without conflict, the embodiments of the present utility model and features of the embodiments may be combined with each other.
In the description of the present utility model, the terms "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", etc. refer to the orientation or positional relationship based on that shown in the drawings, merely for convenience of description of the present utility model and do not require that the present utility model must be constructed and operated in a specific orientation, and thus should not be construed as limiting the present utility model. The terms "coupled" and "connected" as used herein are to be construed broadly and may be, for example, fixedly coupled or detachably coupled; either directly or indirectly through intermediate components, the specific meaning of the terms being understood by those of ordinary skill in the art as the case may be.
As shown in fig. 1, according to an embodiment of the present utility model, there is provided a system for preparing sodium sulfite by recycling active desulfurization rich gas, the system for preparing sodium sulfite comprising:
pretreatment system 1, pretreatment system is used for purifying, cooling and gas-solid separation of active coke regeneration gas, in the specific embodiment of the utility model, pretreatment system 1 comprises a scrubber for purifying gas to remove SO in active coke regeneration gas 3 HCl, HF and dust, and simultaneously realizing gas cooling and gas-solid separation, and removing dust in the flue gas; preferably, the scrubber comprises a primary scrubber 11 and a secondary scrubber 12 connected in sequence, wherein the primary scrubber 11 is used for purifying active coke regeneration gas to primarily remove SO therein 3 HCl, HF and dust and preliminarily realizing gas cooling; the secondary scrubber 12 is used to again purify the gas from the primary scrubber 11 to further remove SO therefrom 3 HCl, HF and dust, further realizing gas cooling, and simultaneously removing fog drops in the gas after the secondary purification; the primary scrubber 11 and the secondary scrubber 12 are used for purifying, cooling and gas-solid separation of the regenerated gas to obtain pretreated gas with high sulfur dioxide purity.
In the specific embodiment of the utility model, the desulfurization rich gas after desulfurization and denitrification analysis of the active coke enters the lower part of the primary scrubber 11, and the gas inlet position is positioned above the washing liquid arranged at the bottom of the primary scrubber 11; the upper part of the primary scrubber 11 is provided with a vortex generating device for generating a rotating vortex for the washing liquid entering the primary scrubber 11, preferably, a first vortex generating device 111 and a second vortex generating device 112 are arranged in the primary scrubber 11 from top to bottom (in the prior art, see the patent of application number 200720195551.3), the primary scrubber 11 is externally provided with a washing circulating pump 13, the washing liquid at the bottom of the primary scrubber 11 enters the first vortex generating device 111 and the second vortex generating device 112 respectively through the washing circulating pump 13, and the two-layer spraying device can cool the upstream regeneration gas entering from the lower part of the primary scrubber 11 and remove impurities and dust. Under the action of the vortex generating device, the washing liquid generates a transient vortex liquid suspension layer, then downward rotating liquid flow with a certain speed is formed, the gas forms upward rotating gas flow with a certain speed, the rotating liquid flow and the rotating gas flow are in impact blending, the liquid phase and the gas phase are in strong blending, the blending strength and the residence time of the washing liquid are increased, impurities are further absorbed under the action of rotary cutting impact, and the impurity removal rate is improved. The arrangement of the vortex generating device greatly increases the gas-liquid contact area and the contact time, and improves the washing efficiency.
The washing circulation pump 13 arranged in the primary scrubber 11 fully absorbs and removes SO in the regeneration gas for the circulating flow of the washing liquid 3 HCl, HF, dust, etc., to convert SO 2 The gas is remained in the gas treated by the primary scrubber 11, most of fluoride, chloride, dust, ammonia and salt substances in the regenerated gas are absorbed by the scrubbing liquid in the process, and the gas temperature is reduced from 350-420 ℃ to 60-85 ℃. The washing liquid is process water, acid gas such as sulfur trioxide is mainly removed, and sulfur dioxide gas cannot be absorbed by the washing liquid.
The unabsorbed gas after passing through the primary scrubber 11 enters from the lower part of the secondary scrubber 12, the secondary scrubber 12 comprises a scrubbing section 121 (also called a lower scrubbing section), a filling section 122, a scrubbing section 121 (also called an upper scrubbing section) and an electric demisting section 123 from bottom to top, and is used for further purifying the gas and separating gas from liquid to remove impurity components, dust and SO in the flue gas 3 Increase SO 2 Is the purity of (1); the gas discharged from the primary scrubber 11 enters a secondary scrubber, and an inlet for receiving the gas discharged from the primary scrubber 11 is arranged above the lower-layer scrubbing section 121 and below the filling section 122; the washing liquid in the secondary washer 12 is circulated from the lower washing stage to the upper washing stage and sprayedSprinkling, namely filling washing liquid in the lower washing section; the purpose of the packing section 122 is to make the washing liquid in the washing section 121 fully contact with the upward rich gas, and impurities in the rich gas are continuously removed by mutual collision with the packing; the filler of the filler section 122 is inclined suspension type porous suspension filler (MBBR) and is made of polytetrafluoroethylene; the rich gas passing through the filling section 122 enters the washing section 121 positioned above the filling section again, and the residence time of the rich gas is prolonged by the reverse contact with the washing liquid, so that the washing effect is ensured; the rich gas passing through the upper washing section 121 enters the electric demisting section 123, fine particles in the rich gas are removed through the electric demisting section 123, namely, the water content in the rich gas is reduced, and the quality of the rich gas is further ensured. Preferably, a washing circulation pump 13 and a cooler 14 for circulating the washing liquid and cooling the gas of the lower washing stage 121 are further provided at the outside of the lower washing stage 121, respectively; the washing liquid in the secondary washer 12 is the same process water as the washing liquid in the primary washer 11. The principle of operation of the cooler 14 is: cooling water is introduced from the outside to enter the cooler 14, and the circulating washing liquid is cooled when passing through the cooler 14, so that indirect heat exchange is performed between the circulating washing liquid and the flue gas, and the temperature of the flue gas is reduced. The gas passes through a packing section 122, a washing section 121 (i.e. an upper washing section) and an electric demisting section 123 in the secondary scrubber 12 in sequence, and the dust and total salt content of the clean gas leaving the secondary scrubber 12 is less than 5mg/m 3 The gas then enters the reaction recovery system 2. Preferably, the gas is sent to the reaction recovery system 2 after being pressurized by the tail gas fan 29. When the concentration of ammonium salt in the washing liquid at the bottom of the secondary scrubber 12 reaches a set value, the ammonium salt is periodically discharged to the wastewater tank 15 by a wastewater discharge pump.
The reaction recovery system 2 comprises a reaction unit and a recovery unit, and the reaction unit of the reaction recovery system 2 is connected with a gas outlet of the pretreatment system 1 and is used for synthesizing and recovering sodium sulfite in a reaction manner; the reaction unit of the reaction recovery system 2 comprises a reaction device; the recovery unit comprises a centrifugal device and a drying device, and the reaction device is connected with a gas outlet of the pretreatment system 1 and is used for synthesizing sodium sulfite slurry through reaction.
In the specific embodiment of the utility model, the reaction device comprises a first-stage reactor 21 and a second-stage reactor 22, the pretreated gas enters the first-stage reactor 21, and the upper gas outlet of the first-stage reactor 21 is connected to the upper gas inlet of the second-stage reactor 22 through a first gas pipeline 211; the first gas transmission pipeline 211 is used for transmitting the sulfur dioxide-containing gas from the primary reactor 21 to the secondary reactor 22; the bottom slurry outlet of the primary reactor 21 is connected to the evaporative concentration system 3 by a pipe; the lower slurry outlet of the secondary reactor 22 is connected to the upper slurry inlet of the primary reactor 21 by a first transfer line 212, the first transfer line 212 being used to transfer reacted slurry from the secondary reactor 22 to the primary reactor 21. Preferably, the reaction unit also comprises an alkali liquor tank 23, the secondary reactor 22 is connected with the alkali liquor tank 23, and the alkali liquor in the alkali liquor tank 23 is periodically supplied into the secondary reactor 22; preferably, the lye in the lye tank 23 is soda lye, i.e. sodium carbonate solution, preferably sodium carbonate solution with a mass concentration of 20-30% (e.g. 21%, 22%, 23%, 24%, 25%, 26%, 27%, 28%, 29%) is used. Still preferably, the secondary reactor 22 is provided with a circulating pump 5 for self-circulating slurry in the reactor, and the secondary reactor 22 is circularly absorbed by the circulating pump 5, SO that gas and liquid can be fully contacted and SO can be fully absorbed 2 . According to the utility model, the primary reactor 21 outputs the finished product liquid (sodium sulfite slurry), the concentration of sulfur dioxide in the flue gas in the primary reactor 21 is highest, the flue gas is easy to absorb, repeated absorption is not needed, so that the primary reactor 21 does not need to be provided with a circulating pump 5, the sulfur dioxide in the flue gas in the secondary reactor 22 is reduced, and the absorption rate can be improved only by circulating the solution.
The purified gas passing through the secondary scrubber 12 enters the primary reactor 21 to carry out synthesis reaction, and the residual gas exiting the primary reactor 21 enters the secondary reactor 22 to further carry out reaction SO 2 The gas is further absorbed; the liquid level of the primary reactor 21 is periodically replenished from the secondary reactor 22, the liquid level of the secondary reactor 22 is periodically replenished from the alkali liquid tank 23, and the SO in the solution is gradually increased 2 Concentration, absorption in solutionSO of (2) 2 Maximizing the concentration of (2); the unabsorbed gas in the final secondary reactor 22 is sent to the tail gas treatment system 4. Preferably, the primary reactor 21 and the secondary reactor 22 are provided with a gas outlet communicated with the tail gas treatment system 4, a sodium sulfite slurry outlet communicated with the evaporation concentration system 3 and a gas inlet communicated with the gas outlet of the pretreatment system 1, so that gas and liquid can directly enter and exit from the primary reactor 21 and the secondary reactor 22, and the discharging of the other reactor is not influenced once one reactor fails.
Evaporative concentration System 3 the evaporative concentration System 3 includes a heater 31, a separator 32, a condenser 34 and a vacuum pump 35. The generation temperature of the sodium sulfite slurry needs to be high at 150-160 ℃, the generation temperature can not be reached only through the reaction temperature of the reaction device, the yield of the sodium sulfite is low, the efficiency is low, the sodium sulfite slurry can be heated, evaporated and concentrated through the evaporation and concentration system, the generation amount of the sodium sulfite is improved, the yield is improved, and the cost is reduced. The heater 31 comprises a tube side and a shell side, the tube side is used for storing slurry, the shell side is used for storing hot steam, the heater 31 is connected with a bottom slurry outlet of the primary reactor 21, the slurry enters the tube side (the slurry PH in the primary reactor 21 is 7.7-8.2 and the discharged slurry enters the tube side when the discharged slurry reaches 65-75 ℃), and the sodium sulfite slurry is heated, evaporated and concentrated through steam heat exchange of the tube side and the shell side. The separator 32 is connected with the condenser 34, the condenser 34 is connected with the vacuum pump 35, the negative pressure is kept in the condenser 34 through the suction effect of the vacuum pump 35, and the micro negative pressure is kept in the separator 32. The concentrated slurry enters the separator 32 under the action of pressure difference, the inlet of the separator 32 is connected with the tube side outlet of the heater 31, the sodium sulfite slurry enters the separator 32 and is subjected to gas-liquid separation through flash evaporation, and the bottom slurry circulation outlet of the separator 32 conveys the slurry to the tube side bottom inlet of the heater 31 through the evaporation circulating pump 33, so that the slurry is continuously subjected to circulation evaporation concentration between the heater 31 and the separator 32; the bottom concentrated slurry outlet of the separator 32 is connected to a centrifugal device, and concentrated slurry which has been concentrated by multiple evaporation to a certain concentration enters the centrifugal device. The upper steam outlet of the separator 32 and the upper steam outlet of the shell side of the heater 31 are connected with a condenser 34, and the condenser 34 is used for cooling the steam; the condenser 34 also includes a tube side through which condensation takes place and a shell side to which the circulating cooling water is connected. The saturated steam is used as a heat source, enters the shell side of the heater 31 for heat exchange and condensation, and enters the condenser 34 for condensation together with the secondary steam generated by the separator 32, and is pumped by the vacuum pump 35.
Preferably, the vacuum pump 35 is connected with the vacuum tank 36, the vacuum tank 36 plays a role in buffering, the vacuum tank 36 is vacuumized through the action of the vacuum pump 35, the top outlet and the bottom outlet of the condenser 34 are connected to the vacuum tank 36, the top outlet of the condenser 34 is communicated with the vacuum tank 36, the condenser 34 is in a negative pressure environment, condensed water is cooled in the condenser 34 and is conveyed into the vacuum tank 36 through the bottom outlet, and the cooling recovery process of steam is completed.
The concentrated sodium sulfite slurry after the heating separation and concentration enters a centrifugal device from a separator 32 for solid-liquid separation, and a filter cake enters a drying device to obtain solid sodium sulfite powder.
In an embodiment of the utility model, the reaction recovery system 2 further comprises a mother liquor tank 24, the liquid generated by the centrifugal device and the tail gas treatment system 4 is conveyed into the mother liquor tank 24, and the mother liquor tank 24 can convey the liquid into the alkali liquor tank 23 through a mother liquor transfer pump. The liquid in the mother liquor tank 24 is the absorption part SO 2 The slurry of the gas can be conveyed to the alkali liquid tank 23 for further utilization, thereby realizing the maximum utilization of resources.
Still preferably, the mother liquor after centrifugal separation is sent to a mother liquor tank 24, and the filter cake enters a drying device through a chute.
In the specific embodiment of the utility model, the drying device comprises an air dryer 27 and a cyclone collector 28, and the material dried by the air dryer 27 enters the cyclone collector 28 for particle collection; preferably, the cyclone collector 28 is a two-stage cyclone collector 28. Further preferably, a drying feeder 26 is further arranged before the air dryer 27, the drying feeder 26 is an internal drying sealing space, and the filter cake enters the internal drying space of the drying feeder 26 and is transported to the air dryer 27.
And the tail gas treatment system 4 is used for purifying the tail gas generated after passing through the reaction device, the centrifugal device and the drying device so as to further absorb sulfur dioxide and dust in the tail gas. In the specific embodiment of the utility model, the residual gas in the secondary reactor 22 and the residual gas in the cover body where the centrifugal separator 25 is positioned are both conveyed to the tail gas treatment system 4; preferably, the residual gas generated by the second stage cyclone collector 28 is sent to the tail gas treatment system 4 by an induced draft fan 210; preferably, the residual gas generated inside the soda ash tank (i.e., the soda ash tank 23) also enters the tail gas treatment system 4 for purification treatment.
In the specific embodiment of the utility model, the tail gas treatment system 4 comprises a tail gas absorption tower 41, an alkali liquid pool is arranged at the bottom of the tail gas absorption tower 41, residual gas enters from the lower part of the tail gas absorption tower 41, an inlet of the residual gas is arranged above alkali liquid at the bottom of the tail gas absorption tower, a circulating pump 5 is arranged outside the tail gas absorption tower 41, the alkali liquid at the bottom of the tail gas absorption tower 41 is conveyed to the top for spraying and continuously circulates, and the sprayed alkali liquid is in contact with the upward tail gas in a descending manner. When the pH value or concentration of the alkali liquor continuously circulated reaches a certain value, the alkali liquor is periodically conveyed to the mother liquor tank 24; the gas purified by the tail gas absorption tower 41 is discharged through the high altitude, and reaches the atmospheric emission standard. The alkali liquid in the alkali liquid pool at the bottom of the tail gas absorption tower 41 is soda ash liquid, namely sodium carbonate solution, and sodium carbonate solution with the mass concentration of 20-30% (such as 21%, 22%, 23%, 24%, 25%, 26%, 27%, 28%, 29%) is preferably adopted.
In order to further understand the system for preparing sodium sulfite by recycling the active pyro-desulfurization rich gas, the utility model also provides a method for preparing sodium sulfite by recycling the active pyro-desulfurization rich gas, which comprises the following steps:
step one, pretreatment of regeneration gas, comprising:
after the regeneration gas after desulfurization, denitrification and analysis of the active coke is subjected to washing, cooling and gas-solid separation by a primary scrubber 11 and a secondary scrubber 12 of the pretreatment system 1, SO is removed 3 And (3) obtaining pretreated gas with high sulfur dioxide purity after impurities such as HCl, HF and dust.
Step two, synthesizing, evaporating, concentrating and recycling the product, comprising the following steps:
the pretreated gas is pressurized by a tail gas fan 29 and then enters a first-stage reactor 21, residual gas in the first-stage reactor 21 enters a second-stage reactor 22, slurry after sulfur dioxide is absorbed in the second-stage reactor 22 is periodically replenished with liquid in the first-stage reactor 21, and soda liquid in a soda liquid tank 23 is periodically replenished in the second-stage reactor 22; and the secondary reactor 22 continuously and circularly absorbs sulfur dioxide gas through the circulating pump 5; when the reaction of the first-stage reactor 21 reaches the end (when the PH of the solution in the first-stage reactor 21 is 7.7-8.2 and the temperature of the discharged material reaches 65-75 ℃), the system closes the raw material inlet valve, opens the liquid discharge valve, discharges the slurry into the tube side of the heater 31, and carries out heat exchange, evaporation and concentration on the slurry through the steam of the shell side; the vacuum pump 35 is opened, vacuum is pumped, the condenser 34 and the separator 32 are in a negative pressure state, the concentrated slurry enters the separator 32 and is further concentrated through gas-liquid separation, then the slurry is continuously concentrated in a circulating way between the heater 31 and the separator 32 under the action of the evaporation circulating pump 33, and the steam is cooled and condensed by the condenser 34 and is recovered.
The slurry in the separator 32 is periodically discharged into a centrifugal device, and after centrifugal separation by the centrifugal device, the mother liquor is conveyed to the mother liquor tank 24, the filter cake enters the drying feeder 26, is conveyed to the air dryer 27 by the drying feeder 26 for drying, and then enters the two-stage cyclone collector 28 to collect sodium sulfite powder particles.
Step three, tail gas treatment, which comprises the following steps:
the tail gas generated in the secondary reactor 22, the centrifugal device, the secondary cyclone collector 28 and the alkali liquor tank 23 enters the tail gas treatment system 4 to be washed and purified by alkali liquor sodium carbonate solution, alkali liquor in the washing tower is continuously and circularly sprayed from bottom to top, the concentration of the circulated alkali liquor reaches a certain value and then is periodically conveyed to the mother liquor tank 24, the liquid in the mother liquor tank 24 is conveyed into the alkali liquor tank 23, and the resource utilization is maximized; and (5) after the gas is purified, emptying the gas at high altitude.
In summary, the system and the method for preparing the sodium sulfite by recycling the active coke desulfurization rich gas have the following excellent effects: the primary reactor and the secondary reactor are communicated and shared, so that the primary reaction can be stabilizedThe reaction time of the reactor reduces the influence of the reactor fault on the discharge of the primary reactor, is beneficial to the continuous and stable operation of a downstream evaporation concentration system, a centrifugal separation system and a drying system, and increases the SO absorbed by the primary reactor 2 The concentration of the alkali liquor is reduced, and the method is beneficial to the reduction of the energy consumption of the system and the improvement of the product quality.
The sodium sulfite powder product can be continuously produced, the continuous production requirement is met, the purity of the obtained sodium sulfite powder product is more than 90 percent, and the industrial use standard is met.
The two-stage vortex generating device is adopted to generate circulating rotary liquid flow to continuously wash the flue gas, SO that better absorption and purification effects and SO (SO) can be achieved 2 The loss rate is lower.
The absolute circulation quantity of the circulating absorption liquid is effectively reduced by adopting a two-stage absorption method, and simultaneously SO in the waste gas is improved 2 Is SO using the method and system of the present utility model 2 The absorption rate of the alkali liquor is more than 98%, the consumption of the alkali liquor is lower, and the treated gas can be directly discharged into the atmosphere to meet the emission standard.
The pretreatment system is relatively independent and has no related interlocking relation with the later reaction recovery system, and when the pretreatment system fails, the pretreatment system can be directly replaced by a standby device, so that the influence on a downstream sodium sulfite powder product preparation system is reduced.
The above description is only of the preferred embodiments of the present utility model and is not intended to limit the present utility model, but various modifications and variations can be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (10)
1. A system for preparing sodium sulfite by recycling active coke desulfurization rich gas, which is characterized by comprising:
the pretreatment system is used for purifying, cooling and gas-solid separation of the regenerated gas to obtain pretreated gas with higher sulfur dioxide purity;
the reaction recovery system comprises a reaction unit and a recovery unit, and the reaction unit of the reaction recovery system is connected with a gas outlet of the pretreatment system and is used for synthesizing and recovering sodium sulfite in a reaction manner;
the evaporation concentration system is connected with the outlet of the reaction unit and is used for circularly evaporating and concentrating sodium sulfite slurry generated by the reaction unit, and the sodium sulfite slurry subjected to evaporation concentration enters from the inlet of the recovery unit of the reaction recovery system so as to be recovered;
the tail gas treatment system is connected with a tail gas outlet of the reaction recovery system and is used for purifying the tail gas generated in the reaction recovery system so as to further absorb sulfur dioxide and dust in the tail gas;
the pretreatment system includes: scrubber for purifying gas to remove SO in regeneration gas 3 HCl, HF and dust, and simultaneously realizing gas cooling and gas-liquid separation;
the scrubber comprises two stages of scrubbers which are connected in sequence, wherein the first stage of scrubber is used for purifying active coke regeneration gas to primarily remove SO therein 3 HCl, HF and dust and preliminarily realizing gas cooling; the secondary scrubber is used for purifying the gas from the primary scrubber again to further remove SO therein 3 HCl, HF and dust, further realizing gas cooling, and simultaneously removing fog drops in the gas after the secondary purification;
the upper part of the inside of the primary scrubber is provided with a vortex generating device, and the vortex generating device is provided with a first vortex generating device and a second vortex generating device which are arranged on an upper layer and a lower layer respectively; the outside of the primary scrubber is provided with a washing circulating pump, and washing liquid at the bottom of the primary scrubber enters the vortex generating device through the washing circulating pump to generate a transient vortex liquid suspension layer and then forms a downward running rotating liquid flow to perform impact reaction with the upward regeneration gas;
the secondary scrubber comprises a scrubbing section, a filling section, a scrubbing section and an electric demisting section from bottom to top, wherein the filling of the filling section is inclined suspension type porous suspension filling which is made of polytetrafluoroethylene; the outside of the washing section is also provided with a washing circulating pump and a cooler which are respectively used for circulating washing liquid and cooling gas of the washing section;
the content of gas dust and total salt passing through the secondary scrubber is less than 5mg/m 3 ；
The reaction unit of the reaction recovery system comprises a reaction device, wherein the reaction device comprises a primary reactor and a secondary reactor, and the secondary reactor is provided with a circulating pump for self-circulation of slurry;
the secondary reactor is connected with an alkali liquor tank, and alkali liquor in the alkali liquor tank is periodically conveyed to be replenished into the secondary reactor; the recovery unit includes: a centrifugal device; the reaction unit further comprises a mother liquor tank, the liquid generated by the centrifugal device and the tail gas treatment system is conveyed into the mother liquor tank, and the liquid in the mother liquor tank is conveyed into the alkali liquor tank through a pipeline.
2. The system for preparing sodium sulfite by recycling active coke desulfurization rich gas as claimed in claim 1, wherein the reaction unit of the reaction recovery system comprises:
the reaction device is connected with a gas outlet of the pretreatment system and is used for synthesizing sodium sulfite by reaction;
the recovery unit includes: the centrifugal device is connected with a concentrated slurry outlet of the evaporation concentration system and is used for recovering solid materials containing the sodium sulfite; the drying device is connected with the solid outlet of the centrifugal device and is used for drying the solid material containing the sodium sulfite;
the pretreated gas enters the primary reactor, and an upper gas outlet of the primary reactor is connected to an upper gas inlet of the secondary reactor through a first gas pipeline; the first gas pipeline is used for conveying gas containing sulfur dioxide; the bottom slurry outlet of the primary reactor is connected to the evaporation concentration system through a pipeline; the lower slurry outlet of the secondary reactor is connected to the upper slurry inlet of the primary reactor by a first transfer line for transporting slurry.
3. The system for preparing sodium sulfite by recycling active coke desulfurization rich gas as claimed in claim 2, wherein the evaporation concentration system comprises:
the heater comprises a tube side and a shell side, wherein the tube side is used for storing slurry, the shell side is used for storing hot steam, and the heater is connected with a bottom slurry outlet of the primary reactor and is used for heating, evaporating and concentrating sodium sulfite slurry;
the inlet of the separator is connected with the tube side outlet of the heater, the separator is used for carrying out gas-liquid separation on the sodium sulfite slurry, and the bottom circulating slurry outlet of the separator conveys the slurry to the tube side bottom inlet of the heater through an evaporation circulating pump so as to continuously and circularly evaporate the slurry; the bottom concentrated slurry outlet of the separator is connected with the centrifugal device;
the upper steam outlet of the separator and the shell side upper steam outlet of the heater are connected with the condenser, and the condenser is used for cooling the steam from the separator and the heater;
the vacuum pump is connected with the condenser to form negative pressure in the condenser; a negative pressure is also established in the separator.
4. The system for producing sodium sulfite by recycling active coke desulfurization rich gas as claimed in claim 3, wherein the vacuum pump is connected to the vacuum tank, and a top outlet and a bottom outlet of the condenser are both connected to the vacuum tank.
5. The system for preparing sodium sulfite by recycling active coke desulfurization rich gas as claimed in claim 2, wherein the drying device comprises an air dryer and a cyclone collector, and the material dried by the air dryer enters the cyclone collector for particle collection;
the cyclone collector is a two-stage cyclone collector.
6. The system for preparing sodium sulfite by recycling active coke desulfurization rich gas according to claim 5, wherein a drying feeder is further arranged before the air dryer, and materials enter a drying space inside the drying feeder and are transported to the air dryer.
7. The system for preparing sodium sulfite by recycling 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 alkali liquor at the bottom of the tail gas absorption tower is conveyed to the top and continuously circulated.
8. The method for preparing the sodium sulfite by recycling the active coke desulfurization rich gas is characterized by comprising the following steps of:
step one, pretreatment of regeneration gas, comprising:
purifying the regenerated gas after desulfurization, denitrification and analysis of the active coke by a pretreatment system to obtain pretreated gas with high sulfur dioxide purity;
step two, synthesizing, evaporating, concentrating and recycling the product, comprising the following steps:
the pretreated gas enters a reaction unit of a reaction recovery system, sodium sulfite slurry is prepared by adopting absorption liquid through a two-stage reaction device, and then the sodium sulfite slurry is subjected to evaporation concentration and then centrifugal separation and drying by the recovery unit to obtain sodium sulfite powder particles;
step three, tail gas treatment, which comprises the following steps:
the tail gas generated by the reaction unit and the recovery unit enters the tail gas treatment system, absorption liquid is adopted for washing and purifying again, and the treated gas is exhausted;
the method is carried out with the system according to any one of claims 1 to 7.
9. The method for preparing sodium sulfite by recycling active coke desulfurization rich gas as claimed in claim 8, wherein the pretreated gas enters a reaction unit of the reaction recovery system after being pressurized by a tail gas fan;
the absorption liquid is alkali liquor.
10. The method for preparing sodium sulfite by recycling active coke desulfurization rich gas as claimed in claim 9, wherein the absorption liquid is sodium carbonate solution.
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Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201120251Y (en) * | 2007-11-02 | 2008-09-24 | 北京中航泰达科技有限公司 | Desulfurising-dusting apparatus of spiral vortex impact stream |
| CN101306319A (en) * | 2008-05-26 | 2008-11-19 | 娄爱娟 | Direct discharging flue gas treatment method |
| CN203006961U (en) * | 2013-01-20 | 2013-06-19 | 伍立君 | Device for preparing sodium metabisulfite and anhydrous sodium sulfite |
| CN203342639U (en) * | 2013-06-20 | 2013-12-18 | 义马煤业集团煤生化高科技工程有限公司 | Recovery treatment device for chemical acid waste gas containing hydrogen sulfide |
| CN105289204A (en) * | 2015-11-23 | 2016-02-03 | 金川集团股份有限公司 | System and method using powdery active cock for processing low concentration sulfur dioxide flue gas |
| CN106178819A (en) * | 2016-08-22 | 2016-12-07 | 朱双跃 | Activated coke desulfurization denitration by-product reforming unit and system for desulfuration and denitration and method |
| CN206103690U (en) * | 2016-10-11 | 2017-04-19 | 江苏齐清环境科技有限公司 | Acyl chlorides chemical industry preface sulfur dioxide exhaust purification recovery unit |
| EP3421115A2 (en) * | 2017-09-22 | 2019-01-02 | Jiangnan Environmental Protection Group Inc. | Apparatus and method for ammonia-based desulfurization |
| CN109876630A (en) * | 2019-03-06 | 2019-06-14 | 株洲三特环保节能股份有限公司 | A method of sulfur dioxide flue gas is administered with alkaline scrap material and recycles tin antimony metal and sodium sulfite crystal |
| 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 |
| CN212024793U (en) * | 2020-01-21 | 2020-11-27 | 北京中航泰达环保科技股份有限公司 | System for sodium sulfite is prepared in rich gas resourceization of active coke desulfurization |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105214457B (en) * | 2014-06-05 | 2018-04-17 | 魏雄辉 | A kind of fume desulfuring and denitrifying Processes and apparatus |
-
2020
- 2020-01-21 CN CN202010072611.2A patent/CN111170339B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201120251Y (en) * | 2007-11-02 | 2008-09-24 | 北京中航泰达科技有限公司 | Desulfurising-dusting apparatus of spiral vortex impact stream |
| CN101306319A (en) * | 2008-05-26 | 2008-11-19 | 娄爱娟 | Direct discharging flue gas treatment method |
| CN203006961U (en) * | 2013-01-20 | 2013-06-19 | 伍立君 | Device for preparing sodium metabisulfite and anhydrous sodium sulfite |
| CN203342639U (en) * | 2013-06-20 | 2013-12-18 | 义马煤业集团煤生化高科技工程有限公司 | Recovery treatment device for chemical acid waste gas containing hydrogen sulfide |
| CN105289204A (en) * | 2015-11-23 | 2016-02-03 | 金川集团股份有限公司 | System and method using powdery active cock for processing low concentration sulfur dioxide flue gas |
| CN106178819A (en) * | 2016-08-22 | 2016-12-07 | 朱双跃 | Activated coke desulfurization denitration by-product reforming unit and system for desulfuration and denitration and method |
| CN206103690U (en) * | 2016-10-11 | 2017-04-19 | 江苏齐清环境科技有限公司 | Acyl chlorides chemical industry preface sulfur dioxide exhaust purification recovery unit |
| EP3421115A2 (en) * | 2017-09-22 | 2019-01-02 | Jiangnan Environmental Protection Group Inc. | Apparatus and method for ammonia-based desulfurization |
| CN109876630A (en) * | 2019-03-06 | 2019-06-14 | 株洲三特环保节能股份有限公司 | A method of sulfur dioxide flue gas is administered with alkaline scrap material and recycles tin antimony metal and sodium sulfite crystal |
| 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 |
| CN212024793U (en) * | 2020-01-21 | 2020-11-27 | 北京中航泰达环保科技股份有限公司 | System for sodium sulfite is prepared in rich gas resourceization of active coke desulfurization |
Non-Patent Citations (2)
| Title |
|---|
| 《化工百科全书》编辑委员会.《化工百科全书 第19卷 油墨－X射线技术》.《化工百科全书》编辑委员会,1998,596-597. * |
| 马广大.大气污染控制工程 第2版.北京：中国环境科学出版社,2004,562-563. * |
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