CN107128884A - A kind of current stabilization state high concentration SO2Flue gas Sulphuric acid method - Google Patents

A kind of current stabilization state high concentration SO2Flue gas Sulphuric acid method Download PDF

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Publication number
CN107128884A
CN107128884A CN201710288991.1A CN201710288991A CN107128884A CN 107128884 A CN107128884 A CN 107128884A CN 201710288991 A CN201710288991 A CN 201710288991A CN 107128884 A CN107128884 A CN 107128884A
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China
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flue gas
concentration
during smelting
catalyst layer
gas during
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Inventor
李大江
袁朝新
郭持皓
梁东东
孙留根
常耀超
张淼
孙聪
余群波
高磊
黄海辉
胡磊
韦其晋
孙彦文
王为振
李云
陶坤
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Beijing General Research Institute of Mining and Metallurgy
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Beijing General Research Institute of Mining and Metallurgy
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Priority to CN201710288991.1A priority Critical patent/CN107128884A/en
Publication of CN107128884A publication Critical patent/CN107128884A/en
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    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/69Sulfur trioxide; Sulfuric acid
    • C01B17/74Preparation
    • C01B17/76Preparation by contact processes
    • C01B17/78Preparation by contact processes characterised by the catalyst used

Abstract

The invention discloses a kind of current stabilization state high concentration SO2Flue gas Sulphuric acid method, as SO in flue gas during smelting in flue gas during smelting or after dilution2Volumetric concentration is 14%~20% and O2With SO2Volume ratio ratio be not less than 0.7 when, according to SO2Volumetric concentration is loaded to the first catalyst layer in converter, so that the exit gas temperature of the first catalyst layer is no more than 640 DEG C, while ensureing that the exit gas temperature of the second catalyst layer second catalyst layer when reaching equilibrium conversion is no more than 640 DEG C;The catalyst layer of remaining in converter realizes maximum conversion rate.The present invention makes SO in flue gas during smelting2Flue gas Sulphuric acid processing just can be directly carried out in higher concentration, the cost of investment and operating cost of acid-producing apparatus can not only be saved, and can take into account that produce load is low, SO2Flue gas Sulphuric acid processing when concentration is smaller.

Description

A kind of current stabilization state high concentration SO2Flue gas Sulphuric acid method
Technical field
The present invention relates to flue gas acid preparing technical field, more particularly to a kind of current stabilization state high concentration SO2Flue gas Sulphuric acid method.
Background technology
At present, metal sulfide ore rich reserves, especially copper mine, nickel minerals and lead ore in nonferrous metal resources.This A little metal sulfide ores can produce substantial amounts of SO during pyrometallurgical smelting2Gas is general to be given using the method for flue gas Sulphuric acid To reclaim.In flue gas process for preparing sulfuric acid, SO2It is converted into SO3Reaction be strongly exothermic reversible reaction, it is necessary at 400~420 DEG C Reaction balance could be approached in the presence of multi-layer catalyst, maximum conversion rate is realized.Under equal flue gas flow, SO2Concentration is higher Then react the heat discharged bigger, but be limited to catalyst activity and equipment intensity, each catalyst layer exit gas temperature Control is required to below 640 DEG C, therefore conventional flue gas process for preparing sulfuric acid enters SO in the flue gas during smelting converted2Volumetric concentration is needed Control is below 14%.
In the late two decades, it is a kind of can improve fuel efficiency, energy-saving oxygen-rich smelting technology is in non-ferrous metal metallurgy Industry is increasingly widely applied, and incident is SO in flue gas during smelting2Concentration is significantly increased, SO2Concentration 18% with Above turn into normality, it is general to use the method that benefit wind dilutes by SO in flue gas2Concentration is reduced to less than 14% and carries out conventional flue gas again Sulphuric acid flow.But mending amount of flue gas emission after wind dilution can be significantly increased, and which results in converting apparatus and the dry specification phase for inhaling equipment It should increase, equipment investment and operating cost are significantly increased.
Meanwhile, many smelting enterprises are limited to various condition elements in actual production, and produce load, which does not often reach, to be set Meter scale, in this case SO in flue gas during smelting2Concentration can decline with the reduction of produce load, and this can cause flue gas sulphur Exothermic heat of reaction amount is converted in acid not enough, it is necessary to open electric furnace or fuel-firing preheating stove to maintain the heat of flue gas system for preparing sulfuric acid to put down Weigh, therefore operating cost can be significantly increased.
The content of the invention
In order to solve to work as SO in existing flue gas process for preparing sulfuric acid2Needed SO during excessive concentration2Volumetric concentration is reduced to 14% Flue gas Sulphuric acid could be carried out below and handles this technical problem, and the invention provides a kind of current stabilization state high concentration SO2Flue gas system Sulfuric acid method, makes SO in flue gas during smelting2Flue gas Sulphuric acid processing just can be directly carried out in higher concentration, can not only be significantly The cost of investment and operating cost of acid-producing apparatus are saved, and can take into account that produce load is low, SO2Flue gas system when concentration is smaller Sulfuric acid treatment.
The purpose of the present invention is achieved through the following technical solutions:
A kind of current stabilization state high concentration SO2Flue gas Sulphuric acid method, including:When in flue gas during smelting or after dilution in flue gas during smelting SO2Volumetric concentration is 14%~20% and O2With SO2Volume ratio ratio be not less than 0.7 when, according to SO2Volumetric concentration is to turning Change the first catalyst layer in device to be loaded, the exit gas temperature of the first catalyst layer is no more than 640 DEG C, while guarantee the The exit gas temperature of two catalyst layers, second catalyst layer when reaching equilibrium conversion is no more than 640 DEG C;Its in converter Remaining catalyst layer realizes maximum conversion rate.
Preferably, flue gas during smelting is made using following methods after described dilution:As SO in flue gas during smelting2Volumetric concentration is big When 14%, into flue gas during smelting, supplement air is diluted, and makes SO in flue gas during smelting2Volumetric concentration be 9%~20% and O2With SO2Volume ratio ratio be not less than 0.7 so that flue gas during smelting after being diluted.
Preferably, as SO in flue gas during smelting in flue gas during smelting or after dilution2When volumetric concentration is 9%~14%, converter In all catalyst layer realize maximum conversion rate.
Preferably, according to SO in flue gas during smelting in flue gas during smelting or after dilution2Volumetric concentration control flue gas acid preparing system exists Switch between three-conversion three-absorption relieving haperacidity flow and double-absorption relieving haperacidity flow;As SO in flue gas during smelting in flue gas during smelting or after dilution2 When volumetric concentration is 12%~20%, control flue gas acid preparing system uses three-conversion three-absorption relieving haperacidity flow;When in flue gas during smelting or dilute Release SO in rear flue gas during smelting2When volumetric concentration is 9%~12%, control flue gas acid preparing system uses double-absorption relieving haperacidity flow.
Preferably, the flue gas during smelting is to remove particulate matter and SO in flue gas by wet scrubbing processing3Smelting cigarette afterwards Gas.
Preferably, the volume flow deviation of described flue gas during smelting is no more than 5%.
Preferably, the input gas temperature of the first described catalyst layer is 400~420 DEG C.
As seen from the above technical solution provided by the invention, the current stabilization state high concentration SO that the present invention is provided2Flue gas system Sulfuric acid method is by the filling scheme of the first catalyst layer of adjustment, and the first catalysis need to only be ensured by making the conversion ratio of the first catalyst layer The exit gas temperature of oxidant layer and the second catalyst layer is no more than 640 DEG C, and without realizing equilibrium conversion, and other are catalyzed Oxidant layer realizes maximum conversion rate, so as to directly to SO2After volumetric concentration is 14%~20% flue gas during smelting or dilution Flue gas during smelting carries out flue gas Sulphuric acid processing, and this can not only ensure SO2Saved with higher total conversion, and significantly The cost of investment and operating cost of acid-producing apparatus.In addition, current stabilization state high concentration SO provided by the present invention2Flue gas Sulphuric acid method Can be according to SO in flue gas during smelting2Volumetric concentration switches between three-conversion three-absorption relieving haperacidity flow and double-absorption relieving haperacidity flow, when SO in flue gas during smelting2Volumetric concentration at 12%~20% (i.e. produce load is larger), can use three-conversion three-absorption relieving haperacidity flow with Realize SO2High conversion, as SO in flue gas during smelting2Volumetric concentration is changeable at 9%~12% (i.e. produce load is smaller) To double-absorption relieving haperacidity flow to maintain the thermal balance of acid making system, without opening electric furnace or fuel-firing preheating stove, fortune is saved Row cost.
Brief description of the drawings
In order to illustrate the technical solution of the embodiments of the present invention more clearly, being used required in being described below to embodiment Accompanying drawing be briefly described, it should be apparent that, drawings in the following description are only some embodiments of the present invention, for this For the those of ordinary skill in field, on the premise of not paying creative work, other can also be obtained according to these accompanying drawings Accompanying drawing.
Fig. 1 is is provided current stabilization state high concentration SO using the embodiment of the present invention 12The flue gas Sulphuric acid of flue gas Sulphuric acid method The schematic diagram of system.
Embodiment
With reference to the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear, complete Ground is described, it is clear that described embodiment is only a part of embodiment of the invention, rather than whole embodiments.Based on this hair Bright embodiment, the every other implementation that those of ordinary skill in the art are obtained under the premise of creative work is not made Example, belongs to protection scope of the present invention.
Below to current stabilization state high concentration SO provided by the present invention2Flue gas Sulphuric acid method is described in detail.
A kind of current stabilization state high concentration SO2Flue gas Sulphuric acid method, including:When in flue gas during smelting or after dilution in flue gas during smelting SO2Volumetric concentration is 14%~20% and O2With SO2Volume ratio ratio be not less than 0.7 when, according to SO2Volumetric concentration is to turning Change the first catalyst layer in device to be loaded, the exit gas temperature of the first catalyst layer is no more than 640 DEG C, while guarantee the The exit gas temperature of two catalyst layers, second catalyst layer when reaching equilibrium conversion is no more than 640 DEG C;Its in converter Remaining catalyst layer realizes maximum conversion rate (maximum conversion rate is the equilibrium conversion close under reaction temperature).
Specifically, current stabilization state high concentration SO2Flue gas Sulphuric acid method can include embodiment in detail below:
(1) flue gas during smelting is to remove particulate matter and SO in flue gas by wet scrubbing processing3Flue gas during smelting afterwards.When SO in flue gas during smelting2When volumetric concentration is more than 14%, into flue gas during smelting, supplement air is diluted, and makes SO in flue gas during smelting2Body Product concentration is 9%~20% and O2With SO2Volume ratio ratio be not less than 0.7 (O2With SO2Volume ratio with SO2Volume is dense The increase of degree and reduce), so that flue gas during smelting after being diluted.As SO in flue gas during smelting in flue gas during smelting or after dilution2Volume When concentration is 9%~14%, all catalyst layers realize maximum conversion rate in converter.
For example:5 sections of catalyst layers are set in one converter, as SO in flue gas during smelting in flue gas during smelting or after dilution2Body When product concentration is 9%~14%, all catalyst layers realize maximum conversion rate in converter;When in flue gas during smelting or diluting SO in flue gas during smelting afterwards2Volumetric concentration is 14%~20% and O2With SO2Volume ratio ratio be not less than 0.7 when, first urges The conversion ratio of agent layer is restricted, less than equilibrium conversion, and with SO2The rise of volumetric concentration and decline, it is ensured that The exit gas temperature of one catalyst layer and the second catalyst layer can (under normal circumstances no more than 640 DEG C:Work as SO2Volume is dense Spend for 14% when the first catalyst layer conversion ratio≤60.9, work as SO2The conversion of first catalyst layer when volumetric concentration is 15% Rate≤57.7, work as SO2Conversion ratio≤54.9 of first catalyst layer, work as SO when volumetric concentration is 16%2When volumetric concentration is 17% Conversion ratio≤52.3 of first catalyst layer, work as SO2Conversion ratio≤49.8 of first catalyst layer when volumetric concentration is 18%, when SO2Conversion ratio≤47.5 of first catalyst layer, work as SO when volumetric concentration is 19%2First catalyst when volumetric concentration is 20% The conversion ratio of layer≤45.5), and the second catalyst layer, the 3rd catalyst layer and the 4th catalyst layer realize maximum conversion rate, The input gas temperature of the first catalyst layer maintains 400~420 DEG C, the import flue gas volume flow of the first catalyst layer simultaneously Basicly stable, the volume flow deviation of flue gas during smelting is no more than 5%.
(2) according to SO in flue gas during smelting in flue gas during smelting or after dilution2Volumetric concentration controls flue gas acid preparing system at three turns Three inhale switching between relieving haperacidity flow and double-absorption relieving haperacidity flow;As SO in flue gas during smelting in flue gas during smelting or after dilution2Volume When concentration is 12%~20% (i.e. produce load is larger), control flue gas acid preparing system uses three-conversion three-absorption relieving haperacidity flow, and this can To realize SO2High conversion (total conversion is up to 99.96%~99.99%), SO in relieving haperacidity tail gas2Concentration is minimum to be down to 100mg/Nm3Below;As SO in flue gas during smelting in flue gas during smelting or after dilution2Volumetric concentration is 9%~12% (i.e. produce load It is smaller) when, control flue gas acid preparing system uses double-absorption relieving haperacidity flow, and (total conversion is about by second of conversion for flue gas 99.7%) vent gas treatment rear discharge up to standard and after absorbing is sent to, and the exiting flue gas of main air blower is drawn and changed with ii heat exchanger Heat, the flue gas after heat exchange returns again to flue gas main road, reaches the purpose of smoke pre-heating, and this can maintain the thermal balance of acid making system, Electric furnace or fuel-firing preheating stove need not be opened, operating cost is saved.Described flue gas acid preparing system can use existing flue gas Flue gas acid preparing system in process for preparing sulfuric acid;Described three-conversion three-absorption relieving haperacidity flow can be used in existing flue gas process for preparing sulfuric acid " 3+1+1 " three-conversion three-absorption relieving haperacidity flow;Described double-absorption relieving haperacidity flow can be used in existing flue gas process for preparing sulfuric acid " 3+1 " double-absorption relieving haperacidity flow.
Compared with prior art, current stabilization state high concentration SO provided by the present invention2Flue gas Sulphuric acid method has following excellent Point:
(1) current stabilization state high concentration SO provided by the present invention2Flue gas Sulphuric acid method leads to the flue gas during smelting situation of fluctuation The mode for crossing supplement air controls the exhaust gas volumn for entering converter in a relatively stable scope, and can directly handle SO2 Volumetric concentration is up to 14%~20% flue gas during smelting, and the only treatable SO of existing flue gas acid preparing technique2Volumetric concentration≤ 14%, therefore current stabilization state high concentration SO provided by the present invention2Flue gas Sulphuric acid method can significantly reduce acid-producing apparatus type selecting, Save equipment investment.
(2) current stabilization state high concentration SO provided by the present invention2Flue gas Sulphuric acid method can be according to SO in flue gas during smelting2Body Product concentration switches between three-conversion three-absorption relieving haperacidity flow and double-absorption relieving haperacidity flow, as SO in flue gas during smelting2Volumetric concentration exists When 12%~20% (i.e. produce load is larger), three-conversion three-absorption relieving haperacidity flow can be used to realize SO2High conversion (total conversion Rate up to 99.96%~99.99%), SO in relieving haperacidity tail gas2Concentration is minimum to be down to 100mg/Nm3Below;When in flue gas during smelting SO2Volumetric concentration can switch to double-absorption relieving haperacidity flow to maintain relieving haperacidity system at 9%~12% (i.e. produce load is smaller) The thermal balance of system, without opening electric furnace or fuel-firing preheating stove, saves operating cost.
As fully visible, the embodiment of the present invention makes SO in flue gas during smelting2Flue gas system just can be directly carried out in higher concentration Sulfuric acid treatment, can not only save the cost of investment and operating cost of acid-producing apparatus, and can take into account that produce load is low, SO2 Flue gas Sulphuric acid processing when concentration is smaller.
In order to more clearly from show technical scheme provided by the present invention and produced technique effect, below with tool The current stabilization state high concentration SO that body embodiment is provided the embodiment of the present invention2Flue gas Sulphuric acid method is described in detail.
Embodiment 1
By taking certain domestic copper smelting plant as an example, the smeltery uses oxygen-rich smelting technology, the output smelting under different produce loads Refining flue gas situation (butt), (wherein table 1~4 is the flue gas during smelting situation under normal produce load, and table 5 is as shown in table 1 below~5 Flue gas during smelting situation under underload produce load):
Table 1:
SO2 SO3 CO2 O2 N2 It is total
kg/h 53570.51 1273.46 4889.66 15099.59 78894.03 152298.68
Nm3/h 18749.68 356.57 2489.28 10569.71 63115.26 95280.5
Volumetric concentration 19.68% 0.37% 2.61% 11.09% 66.24% 100.00%
Table 2:
SO2 SO3 CO2 O2 N2 It is total
kg/h 58016.86 1375.337 5280.833 16307.56 85205.55 166186.1
Nm3/h 20305.9 385.0956 2688.422 11415.29 68164.48 102959.19
Volumetric concentration 19.72% 0.37% 2.61% 11.09% 66.21% 100.00%
Table 3:
SO2 SO3 CO2 O2 N2 It is total
kg/h 62600.19 1485.364 5703.299 15945.88 92022 179423.01
Nm3/h 21910.07 415.9032 2903.496 12328.51 73617.64 111175.62
Volumetric concentration 19.71% 0.37% 2.61% 11.09% 66.22% 100.00%
Table 4:
SO2 SO3 CO2 O2 N2 It is total
kg/h 67733.41 1604.193 6159.563 17221.55 99383.76 193902.05
Nm3/h 23706.7 449.1755 3135.776 13314.79 79507.05 120113.49
Volumetric concentration 19.74% 0.37% 2.61% 11.09% 66.19% 100.00%
Table 5:
SO2 SO3 CO2 O2 N2 It is total
kg/h 34716.37 950.07 3178.279 31084.40 124350.33 194292.95
Nm3/h 12150.73 266.02 1618.032 21759.08 99480.26 135008.10
Volumetric concentration 9.0% 0.20% 1.20% 16.09% 73.68% 100.00%
Using flue gas system for preparing sulfuric acid as shown in Figure 1, and according to current stabilization state high concentration SO provided by the present invention2Flue gas Sulphuric acid method is handled the flue gas during smelting shown in above-mentioned table 1~5, as SO in flue gas during smelting2Volumetric concentration 12%~ When 20% (i.e. produce load is larger), valve 1, valve 3, valve 6 and the valve of flue gas system for preparing sulfuric acid as shown in Figure 1 can control Door 7 is opened, and valve 2, valve 4 and valve 6 are closed, so that the flue gas system for preparing sulfuric acid uses " 3+1+1 " three-conversion three-absorption system Sour flow, that is, convert heat exchanger flow IIIb, I-IV, IIIa-V, II.As SO in flue gas during smelting2Volumetric concentration is 9%~12% When (i.e. produce load is smaller), valve 1, valve 2, valve 4, the and of valve 5 of flue gas system for preparing sulfuric acid as shown in Figure 1 can control Switch blower fan to open, and valve 3, valve 6 and valve 7 are closed, so that the flue gas system for preparing sulfuric acid switches to two turn two of " 3+1 " Relieving haperacidity flow is inhaled, that is, converts heat exchanger flow IIIb, I-IV, IIIa (branch 1)-V, II (branch 2).
The specific treatment process of flue gas system for preparing sulfuric acid as shown in Figure 1 includes:
(1) process 1:Wet scrubbing processing is carried out to flue gas during smelting to remove particulate matter and SO in flue gas3
(2) process 2:Because flue gas during smelting shown in table 1~4 is in the SO in flue gas during smelting after the processing of process 12Volumetric concentration More than 14%, therefore into these four flue gas during smeltings, supplement air is diluted respectively, makes SO in flue gas during smelting2Volumetric concentration is 9%~20% and O2With SO2Volume ratio with SO2The increase of volumetric concentration and reduce, O2With SO2Volume ratio ratio not Less than 0.7, so that flue gas during smelting after being diluted.Flue gas during smelting volume flow after process 1 or process 2 are handled is substantially steady It is fixed, and the volume flow deviation of flue gas during smelting is no more than 5%.And flue gas during smelting shown in table 5 is smelted after the processing of process 1 SO in flue gas2Volumetric concentration need not carry out the processing of process 2 still less than 14%.
Flue gas during smelting shown in table 1~4 is after the processing of above-mentioned two process, and flue gas during smelting situation difference is as follows after dilution (wherein, flue gas during smelting shown in the corresponding table 1 of table 6, flue gas during smelting shown in the corresponding table 2 of table 7, shown in the corresponding table 3 of table 8 shown in table 6~9 Flue gas during smelting, flue gas during smelting shown in the corresponding table 4 of table 9), and flue gas during smelting shown in table 5 is in its flue gas during smelting after the processing of process 1 Situation is as shown in table 10 below:
Table 6:
SO2 CO2 O2 N2 It is total
kg/h 53570.51 4889.66 26800.29 78894.03 164154.5
Nm3/h 18749.68 2489.28 18760.2 93927.12 133926.3
Volumetric concentration 14.00% 1.86% 14.01% 70.13% 100.00%
Table 7:
SO2 CO2 O2 N2 It is total
kg/h 58016.86 5280.833 26147.13 78894.03 168338.9
Nm3/h 20305.9 2688.422 18302.99 94075.37 135372.7
Volumetric concentration 15.00% 1.99% 13.52% 69.49% 100.00%
Table 8:
Table 9:
SO2 CO2 O2 N2 It is total
kg/h 67733.41 6159.563 24957.18 78894.03 177744.2
Nm3/h 23706.7 3135.776 17470.03 95138.65 139451.2
Volumetric concentration 17.00% 2.25% 12.53% 68.22% 100.00%
Table 10:
SO2 CO2 O2 N2 It is total
kg/h 34716.37 3178.279 31084.40 124350.33 193342.87
Nm3/h 12150.73 1618.032 21759.08 99480.26 135008.10
Volumetric concentration 9.00% 1.2% 16.12% 73.68% 100.00%
(3) process 3:For the flue gas during smelting shown in table 10, flue gas system for preparing sulfuric acid as shown in Figure 1 can be directly switch into Double-absorption relieving haperacidity flow, and catalyst layer all in converter realizes maximum conversion rate.For shown in table 6~9 Flue gas during smelting after dilution, flue gas system for preparing sulfuric acid as shown in Figure 1 can use three-conversion three-absorption relieving haperacidity flow, and converter is used 5 sections of catalyst layers, according to SO in table 6~102Volumetric concentration is loaded to the first catalyst layer in converter, makes the first catalysis The exit gas temperature of oxidant layer is no more than 640 DEG C, while ensureing that the second catalyst layer second is catalyzed when reaching equilibrium conversion The exit gas temperature of oxidant layer is no more than 640 DEG C;The specific conversion ratio of first catalyst layer is as shown in table 11 below:
Table 11:
SO in flue gas2Volumetric concentration 14% 15% 16% 17%
The conversion ratio of first catalyst layer 55.2% 51.9% 48.3% 45.2%
The exit gas temperature of first catalyst layer 608.7℃ 606.9℃ 602.5℃ 598.9℃
(4) process 4:The exiting flue gas of first catalyst layer sequentially enters the second catalyst layer, the after heat exchange cooling Three catalyst layers, and the second catalyst layer and the 3rd catalyst layer realize maximum conversion rate;3rd catalyst layer it is specific Conversion ratio is as shown in table 12 below:
Table 12:
SO in flue gas2Volumetric concentration 14% 15% 16% 17%
The conversion ratio of 3rd catalyst layer 93.1% 91.5% 90.3% 89.4%
(5) process 5:The exiting flue gas of 3rd catalyst layer enters one after (being referred to as once to convert flue gas) heat exchange cooling Secondary absorption tower, with SO in 98% sulfuric acid absorption flue gas3, flue gas is into the 4th catalyst layer after heat exchange afterwards, and progress is for the second time Conversion reaction, reaction conversion ratio reaches maximum conversion rate at this temperature (close to equilibrium conversion).Flue gas system as shown in Figure 1 In sulfate system, the exiting flue gas of the 3rd catalyst layer is divided into two articles of branch roads, after a branch road is preheated by IV, IIIa heat exchanger Into the 4th catalyst layer, another article of branch road enters the 5th catalyst layer after being preheated by V, II heat exchanger, two branch roads are by turning Remerged after changing and enter an absorption tower together, be formed as " 3+1 " double-absorption flow to maintain the thermal balance of system, two turns Two total conversions inhaled are up to 99.7%.
(6) process 6:Enter two after exiting flue gas (secondary conversion flue gas can be referred to as) the heat exchange cooling of 4th catalyst layer Secondary absorption tower, with SO in 98% sulfuric acid absorption flue gas3, flue gas is into the 5th catalyst layer after heat exchange afterwards, and progress is for the third time Conversion reaction, reaction conversion ratio reaches maximum conversion rate at this temperature (close to equilibrium conversion);This 5 sections of the converter are urged The total conversion of agent layer is as shown in table 13 below:
Table 13:
SO in flue gas2Volumetric concentration 14% 15% 16% 17%
The total conversion of this 5 sections of catalyst layers 99.99% 99.99% 99.98% 99.97%
(7) process 7:Enter three absorption towers after the exiting flue gas heat exchange cooling of 5th catalyst layer, inhaled with 98% sulfuric acid Receive SO in flue gas3, SO in flue gas afterwards2Concentration is in 100mg/Nm3Hereinafter, national especially discharge index is reached, can be directly discharged into big Gas.
As fully visible, the embodiment of the present invention makes SO in flue gas during smelting2Flue gas system just can be directly carried out in higher concentration Sulfuric acid treatment, can not only save the cost of investment and operating cost of acid-producing apparatus, and can take into account that produce load is low, SO2 Flue gas Sulphuric acid processing when concentration is smaller.
The foregoing is only a preferred embodiment of the present invention, but protection scope of the present invention be not limited thereto, Any one skilled in the art is in the technical scope of present disclosure, the change or replacement that can be readily occurred in, It should all be included within the scope of the present invention.Therefore, protection scope of the present invention should be with the protection model of claims Enclose and be defined.

Claims (7)

1. a kind of current stabilization state high concentration SO2Flue gas Sulphuric acid method, it is characterised in that including:When in flue gas during smelting or smelting after dilution Refine SO in flue gas2Volumetric concentration is 14%~20% and O2With SO2Volume ratio ratio be not less than 0.7 when, according to SO2Volume Concentration is loaded to the first catalyst layer in converter, the exit gas temperature of the first catalyst layer is no more than 640 DEG C, together When ensure the second catalyst layer second catalyst layer when reaching equilibrium conversion exit gas temperature be no more than 640 DEG C;Turn Change remaining catalyst layer in device and realize maximum conversion rate.
2. current stabilization state high concentration SO according to claim 12Flue gas Sulphuric acid method, it is characterised in that after described dilution Flue gas during smelting is made using following methods:As SO in flue gas during smelting2When volumetric concentration is more than 14%, supplement empty into flue gas during smelting Gas is diluted, and makes SO in flue gas during smelting2Volumetric concentration is 9%~20% and O2With SO2Volume ratio ratio be not less than 0.7, so that flue gas during smelting after being diluted.
3. current stabilization state high concentration SO according to claim 1 or 22Flue gas Sulphuric acid method, it is characterised in that when smelting cigarette SO in flue gas during smelting in gas or after dilution2When volumetric concentration is 9%~14%, all catalyst layers are realized most in converter Big conversion ratio.
4. current stabilization state high concentration SO according to claim 1 or 22Flue gas Sulphuric acid method, it is characterised in that according to smelting SO in flue gas during smelting in flue gas or after dilution2Volumetric concentration controls flue gas acid preparing system in three-conversion three-absorption relieving haperacidity flow and two turn two Inhale switching between relieving haperacidity flow;
As SO in flue gas during smelting in flue gas during smelting or after dilution2When volumetric concentration is 12%~20%, control flue gas acid preparing system is adopted With three-conversion three-absorption relieving haperacidity flow;As SO in flue gas during smelting in flue gas during smelting or after dilution2When volumetric concentration is 9%~12%, control Tobacco curing gas acid making system uses double-absorption relieving haperacidity flow.
5. current stabilization state high concentration SO according to claim 1 or 22Flue gas Sulphuric acid method, it is characterised in that described smelting Refining flue gas is to remove particulate matter and SO in flue gas by wet scrubbing processing3Flue gas during smelting afterwards.
6. current stabilization state high concentration SO according to claim 1 or 22Flue gas Sulphuric acid method, it is characterised in that described smelting The volume flow deviation for refining flue gas is no more than 5%.
7. current stabilization state high concentration SO according to claim 1 or 22Flue gas Sulphuric acid method, it is characterised in that described The input gas temperature of one catalyst layer is 400~420 DEG C.
CN201710288991.1A 2017-04-27 2017-04-27 A kind of current stabilization state high concentration SO2Flue gas Sulphuric acid method Pending CN107128884A (en)

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CN110538543A (en) * 2019-08-30 2019-12-06 楚雄滇中有色金属有限责任公司 Method for stably reaching standard of tail gas in initial stage of acid making and coproduction by smelting flue gas

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CN1935322A (en) * 2006-10-13 2007-03-28 金川集团有限公司 Method for recovery sulfur dioxide from smelting smoke
CN103011092A (en) * 2012-12-28 2013-04-03 中国瑞林工程技术有限公司 Technique for preparing sulfuric acid from SO2 by non-equilibrium state high-concentration twice conversion

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CN1268484A (en) * 2000-04-06 2000-10-04 应燮堂 Improvement of high-concentration sulfur dioxide three-conversion three-absorption acid-making process
CN1935322A (en) * 2006-10-13 2007-03-28 金川集团有限公司 Method for recovery sulfur dioxide from smelting smoke
CN103011092A (en) * 2012-12-28 2013-04-03 中国瑞林工程技术有限公司 Technique for preparing sulfuric acid from SO2 by non-equilibrium state high-concentration twice conversion

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Publication number Priority date Publication date Assignee Title
CN110538543A (en) * 2019-08-30 2019-12-06 楚雄滇中有色金属有限责任公司 Method for stably reaching standard of tail gas in initial stage of acid making and coproduction by smelting flue gas
CN110538543B (en) * 2019-08-30 2021-07-13 楚雄滇中有色金属有限责任公司 Method for stably reaching standard of tail gas in initial stage of acid making and coproduction by smelting flue gas

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