CN103301732A - Device and process for recycling and treating hydrogen sulfide-containing chemical acid waste gas - Google Patents
Device and process for recycling and treating hydrogen sulfide-containing chemical acid waste gas Download PDFInfo
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Abstract
The invention belongs to the technical field of chemical waste gas treatment, and mainly relates to a device and a process for recycling and treating hydrogen sulfide-containing chemical acid waste gas. The process for recycling and treating hydrogen sulfide-containing chemical acid waste gas comprises the following steps of: igniting and completely burning the hydrogen sulfide-containing chemical acid waste gas into sulfur dioxide-rich high-temperature flue gas, recycling much heat and adjusting the temperature of the flue gas by cold air, and enabling the flue gas to enter an adsorption tower; completely absorbing the sulfur dioxide in the flue gas by utilizing an alkaline solution, removing less alkaline solution and sulfite contained in the flue gas absorbed by the alkaline solution, and exhausting the demisted pure flue gas to the atmosphere. The sulfite, which is generated by absorbing sulfur dioxide by the alkaline solution, is oxidized, concentrated, crystallized and dried to obtain side product sulfate.
Description
Technical field
The invention belongs to chemical emission and administer technical field, relate generally to a kind of hydrogen sulfide containing chemical industry sour gas and reclaim device and the technology of administering, this device and process portion unit are applicable to the recovery improvement of boiler smoke and the chemical emission of high-load sulfur dioxide simultaneously.
Background technology
At present a lot of to the method for exhuast gas desulfurization hydrogen in chemical industry, the first kind is wet desulphurization.Press the difference of desulfurizing agent, can be divided into liquid absorption method again and absorb oxidizing process two classes.Comprise the chemical absorption method that utilizes alkaline solution, the Physical Absorption method of utilizing organic solvent and the physical chemistry absorption process of utilizing Physical Absorption and chemical solvent simultaneously in the liquid absorption method; Absorbing oxidizing process at present most popular is to cooperate iron processes.But the general equal by-product sulphur of these methods, sulfuric acid or sulfate etc.
Second class is dry desulfurization.Utilize reproducibility and the combustibility of hydrogen sulfide, so that fixedly oxidant or absorbent come desulfurization or directly burning.This method comprises Claus method, non-renewable ADSORPTION IN A FIXED BED method, membrane separation process, sieve method, pressure swing adsorption method, low temperature processing etc., and desulfurizer therefor, catalyst have active carbon, iron oxide, zinc oxide, manganese dioxide etc.General recyclable sulphur, sulfur dioxide, sulfuric acid and sulfate.This method desulfuration efficiency is higher, but equipment investment is big, and desulfurizing agent needs super regeneration or replacing, and sulfur capacity is relatively low, generally is suitable for the meticulous desulfurization of gas.
The hydrogen sulfide that contains that the Coal Chemical Industry industry produces is that main chemical industry sour gas mainly adopts claus process to carry out sulfur recovery improvement, be about to contain the sour gas of hydrogen sulfide in the claus oven internal combustion, make the partial vulcanization hydrogen-oxygen turn to sulfur dioxide, sulfur dioxide generates sulphur with remaining unreacted hydrogen sulfide in the catalyst reaction again.But in this technology, concentration of hydrogen sulfide is crossed to hang down and can be caused device normally to move in the unstripped gas, can't satisfy the needs of long period safety in production, and complicated operation, and occupation area of equipment is big, fluctuation of service.
Summary of the invention
For solving the problem of existing depriving hydrogen sulphide technology, the present invention proposes a kind of hydrogen sulfide containing chemical industry acid waste gas and reclaims controlling device and technology.
The present invention takes following technical scheme to finish its invention task:
A kind of hydrogen sulfide containing chemical industry acid waste gas reclaims controlling device, and described device includes air blast, burner, incinerator, UTILIZATION OF VESIDUAL HEAT IN boiler, drum, decompressor, first grade absorption tower, two-level absorption tower, washing tank, alkali liquid tank, oxidation tank, serum pot, Crystallization Separation system, drying system, packaging system and all kinds of centrifugal pump;
Described air blast, burner, incinerator, UTILIZATION OF VESIDUAL HEAT IN boiler, drum, decompressor constitute to be lighted, burns fully and be converted into the high-temperature gas that is rich in sulfur dioxide, high-temperature gas is lowered the temperature and reclaimed the conversion system of heat hydrogen sulfide containing acid waste gas;
Described boiler feed pump is communicated with drum, decompressor, by the boiler water that out-of-bounds replenishes after described boiler feed pump pressurization, enter described UTILIZATION OF VESIDUAL HEAT IN boiler, boiler water in the UTILIZATION OF VESIDUAL HEAT IN boiler absorbs the saturated vapor of the heat formation high pressure of described high-temperature gas, the output after decompressor is regulated pressure of described saturated steam is out-of-bounds used for out-of-bounds installing;
The exhanst gas outlet of described UTILIZATION OF VESIDUAL HEAT IN boiler is communicated with the stage casing enriching section of described first grade absorption tower, and the cat head of described first grade absorption tower is communicated with the hypomere absorber portion of described two-level absorption tower, and the cat head of described two-level absorption tower is communicated with chimney;
Described first grade absorption tower, two-level absorption tower and absorption liquid feed mechanism constitute the absorbing and converting system to the absorption cleaning that is rich in sulfur dioxide gas and generation sulphite;
Described absorption liquid feed mechanism includes alkali liquid tank, alkali lye replenishment pump, circulation absorption pump I and circulation absorption pump II; Described alkali liquid tank is communicated with circulation absorption pump I and circulation absorption pump II by described alkali lye replenishment pump, makes alkali lye enter described first grade absorption tower, described two-level absorption tower, and replenishes because absorbing the alkali lye that sulfur dioxide consumes; The alkali lye that described alkali liquid tank consumes is by out-of-bounds replenishing, and the fresh water (FW) that out-of-bounds provides is provided, with alkali lye dilution and control in the finite concentration scope;
The epimere absorber portion of described first grade absorption tower and stage casing enriching section cut off by rising gas cap, and the described stage casing enriching section of first grade absorption tower and hypomere liquid storage section are cut off by dividing plate; The bottom, described epimere absorption tower of first grade absorption tower is communicated with by the pipeline in the first grade absorption tower outside with described hypomere liquid storage section, the hypomere liquid storage section bottom of described first grade absorption tower is communicated with circulation absorption pump I, shower in the epimere absorber portion of described circulation absorption pump I and described first grade absorption tower is communicated with, constitute the absorption liquid circulatory system of first grade absorption tower, enter the most of sulfur dioxide in the gas of first grade absorption tower in order to absorption;
The epimere washing section of described two-level absorption tower and hypomere absorber portion cut off by rising gas cap; Described circulation absorption pump II is communicated with the hypomere absorber portion bottom of described two-level absorption tower, simultaneously, shower in the hypomere absorber portion of circulation absorption pump II and described two-level absorption tower is communicated with, constitute the absorption liquid circulatory system of two-level absorption tower, the residue sulfur dioxide that further will enter in the gas of two-level absorption tower absorbs fully;
The epimere washing section bottom of described two-level absorption tower is communicated with the washing tank, shower in the epimere washing section of described washings circulating pump and described two-level absorption tower is communicated with, constitute the washings circulatory system, a small amount of alkali lye contained in the flue gas that enters the two-level absorption tower epimere and sulphite are carried out spray washing;
Described washing tank is communicated with alkali liquid tank in the absorbing and converting system by control valve, and the alkali lye in the washing tank and sulphite enter alkali liquid tank adjusting concentration of lye after reaching finite concentration;
The hypomere liquid storage section bottom of described first grade absorption tower, the hypomere absorber portion bottom of two-level absorption tower all are communicated with oxidation tank by oxidation cycle pump, venturi-type eductors, constitute the sulfite oxidation system; After the sulphite of the absorption liquid in the described absorption liquid circulatory system reaches finite concentration, enter described sulfite oxidation system by control valve, after the pressurization of oxidation cycle pump, enter oxidation tank through venturi-type eductors, be oxidized to the sulfate slurries in the oxidation tank with fully mixing to be incorporated in from described venturi-type eductors inhaled air;
Described oxidation tank is communicated with shower in the enriching section of described first grade absorption tower stage casing by the oxidation cycle pump;
The enriching section bottom, stage casing of described first grade absorption tower is communicated with serum pot, and makes described serum pot by the shower in the stage casing enriching section that concentrates circulating pump, control valve connection first grade absorption tower, constitutes slurries and concentrates the circulatory system;
The bottom of described serum pot is by control valve, discharging pump and Crystallization Separation system connectivity, and the isolated mother liquor of described Crystallization Separation system returns serum pot, after the crystal drying system drying, sends into packaging system, produces sulfate product.
Be provided with air blast in the described conversion system, it is combustion-supporting that the air that is come by air blast enters incinerator, when needs UTILIZATION OF VESIDUAL HEAT IN boiler export flue-gas temperature is low, can draw the temperature of one tunnel air conditioning UTILIZATION OF VESIDUAL HEAT IN boiler export flue gas again from air blast.
Washing section, the shower in the absorber portion of the absorber portion of described first grade absorption tower, enriching section and two-level absorption tower can be arranged to one or more layers.
Utilize the recovery of the recovery controlling device of above-mentioned hydrogen sulfide containing chemical industry acid waste gas to administer technology, to contain the chemical emission of hydrogen sulfide after burning, hydrogen sulfide is converted into sulfur dioxide, absorb through alkali lye again and be converted into sulphite, sulphite is sulfate through air oxidation, reclaim the chemical industry acid waste gas simultaneously and burn the heat formation saturated steam that produces, that is: auxiliary fuel gas and instrument air are after burner is lighted, feed the combustion air that hydrogen sulfide containing acid waste gas and air blast blast, in being rich in the incinerator of air, burn fully and be converted into the high-temperature gas that is rich in sulfur dioxide, after entering that the UTILIZATION OF VESIDUAL HEAT IN boiler reclaims a large amount of heats and regulating temperature by cold air, epimere absorber portion through entering first grade absorption tower behind the enriching section recovery waste heat of the stage casing of first grade absorption tower is sprayed after the absorption liquid that gets off sponges most of sulfur dioxide, discharge the hypomere absorber portion that enters two-level absorption tower from cat head, sprayed after the absorption liquid that gets off further absorbs remaining sulfur dioxide fully by the hypomere absorber portion top of two-level absorption tower, enter the epimere washing section of two-level absorption tower, contained a small amount of alkali lye and sulphite spray the washings washing of getting off through the epimere washing section of two-level absorption tower in the flue gas, enter atmosphere from chimney after demist.
Described alkali lye can be one or more chemical substances water-soluble or with water generation chemical reaction after formed be alkalescence solution, described chemical substance can be liquefied ammonia, ammoniacal liquor, NaOH, sodium carbonate, magnesia, calcium oxide, calcium hydroxide etc.Different alkaline solution absorbs sulfur dioxide and after air oxidation, formation be corresponding sulfate, when using liquefied ammonia, ammoniacal liquor, form ammonium sulfate; When using NaOH, sodium carbonate, form sodium sulphate; When using calcium oxide, calcium hydroxide, form calcium sulfate.
Fresh water (FW) enters behind the washing tank by the washings circulating pump and gets to shower in the epimere washing section of two-level absorption tower, and washings spray downwards, return the washing tank behind the washing flue gas, and flue gas is carried out circulation cleaning.Alkali lye in the washing tank and sulphite enter alkali liquid tank adjusting concentration of lye after reaching finite concentration.
The alkali lye of absorption liquid for being provided by alkali liquid tank in described first grade absorption tower, the two-level absorption tower absorption liquid circulatory system; The alkali lye that alkali liquid tank comes is squeezed into shower in the hypomere absorber portion of shower in the first grade absorption tower epimere absorber portion, two-level absorption tower respectively after the pressurization of alkali lye replenishment pump and through circulation absorption pump I and circulation absorption pump II, the gas that is rich in sulfur dioxide is carried out absorption cleaning; The epimere absorber portion of first grade absorption tower bottom absorption liquid imports the hypomere liquid storage section of first grade absorption tower, the epimere absorber portion of first grade absorption tower, the hypomere absorber portion of two-level absorption tower are squeezed into by circulation absorption pump I and circulation absorption pump II respectively in the hypomere absorber portion bottom of two-level absorption tower, to the gas that the is rich in sulfur dioxide absorption cleaning that circulates; Sulphite in the described absorption liquid reaches finite concentration, at the bottom of tower, discharge by after the pressurization of oxidation cycle pump, enter oxidation tank through venturi-type eductors, fully mix to be incorporated in the venturi-type eductors inhaled air and be oxidized to sulfate in the oxidation tank, send into the shower of first grade absorption tower stage casing enriching section, the hot flue gas heating that sulfate liquor is come in by the bottom concentrates the back from the stage casing enriching section bottom inflow serum pot of first grade absorption tower; Concentrate circulating pump and squeeze into shower in the enriching section of first grade absorption tower stage casing after the pressurization of the slurries in the serum pot, behind the hot flue gas heating evaporation that spray downwards, large quantity of moisture are come in by the bottom, slurries flow into serum pot and continue the circulation enrichment from the bottom; Sulfate slurries in the serum pot reach capacity and send into the Crystallization Separation system by discharging pump, return serum pot from the isolated mother liquor of Crystallization Separation system, after the crystal drying system drying, the sulfate quality is up to state standards, send into packaging system, produce qualified sulfate product.
A kind of hydrogen sulfide containing chemical industry acid waste gas that the present invention proposes reclaims controlling device and technology, take technique scheme hydrogen sulfide containing chemical emission can be converted into valuable sulfate product, reclaim chemical emission and burned the heat that produces, reached the purpose of administering waste gas and heat recovery simultaneously.
Description of drawings
Accompanying drawing 1 is device of the present invention and process chart.
Accompanying drawing 2, accompanying drawing 3 are respectively device and the process chart of embodiment 2, embodiment 3.
Among the figure: 1, air blast, 2, burner, 3, incinerator, 4, the UTILIZATION OF VESIDUAL HEAT IN boiler, 5, drum, 6, boiler feed pump, 7, decompressor, 8, first grade absorption tower, 9, two-level absorption tower, 10, chimney, 11, circulation absorption pump I, 12, circulation absorption pump II, 13, the washing tank, 14, the washings circulating pump, 15, alkali liquid tank, 16, the alkali lye replenishment pump, 17, venturi-type eductors, 18, oxidation tank, 19, the oxidation cycle pump, 20, serum pot, 21, concentrate circulating pump, 22, discharging pump, 23, the Crystallization Separation system, 24, drying system, 25, packaging system, 26, boiler water, 27, nitrogen, 28, the sulfide hydrogen acid waste gas, 29, auxiliary fuel gas, 30, instrument air, 31, fresh water (FW), 32, alkali lye, 33, air.
The specific embodiment
With specific embodiment the present invention is illustrated by reference to the accompanying drawings:
Embodiment 1
As shown in Figure 1, a kind of hydrogen sulfide containing chemical industry acid waste gas reclaims controlling device and technology, and described device includes air blast 1, burner 2, incinerator 3, UTILIZATION OF VESIDUAL HEAT IN boiler 4, drum 5, first grade absorption tower 8, two-level absorption tower 9, washing tank 13, alkali liquid tank 15, oxidation tank 18, serum pot 20, Crystallization Separation system 23, drying system 24, packaging system 25 and all kinds of centrifugal pump.
Described burner 2, incinerator 3, UTILIZATION OF VESIDUAL HEAT IN boiler 4, drum 5, boiler feed pump 6, decompressor 7 constitutes to be lighted, burns fully and be converted into the high-temperature gas that is rich in sulfur dioxide, high-temperature gas is lowered the temperature and reclaimed the conversion system of heat hydrogen sulfide containing acid waste gas.
Described boiler feed pump 6 is communicated with drum 5, decompressor 7, after described boiler feed pump 6 pressurizations, enters described UTILIZATION OF VESIDUAL HEAT IN boiler 4 by the boiler water 26 that out-of-bounds replenishes.Boiler water in the UTILIZATION OF VESIDUAL HEAT IN boiler 4 absorbs the saturated vapor of the heat formation high pressure of described high-temperature gas, and the output after decompressor 7 is regulated pressure of described saturated steam is out-of-bounds used for out-of-bounds installing.
The exhanst gas outlet of described UTILIZATION OF VESIDUAL HEAT IN boiler 4 is communicated with the stage casing enriching section of described first grade absorption tower 8, and the cat head of described first grade absorption tower 8 is communicated with the hypomere absorber portion of described two-level absorption tower 9, and the cat head of described two-level absorption tower 9 is communicated with chimney 10.
Described first grade absorption tower 8, two-level absorption tower 9 and absorption liquid feed mechanism constitute the absorbing and converting system to the absorption cleaning that is rich in sulfur dioxide gas and generation sulphite.
Described absorption liquid is alkaline solution, can be one or more chemical substances water-soluble or with water generation chemical reaction after form be alkalescence solution, described chemical substance can be liquefied ammonia, ammoniacal liquor, NaOH, sodium carbonate, magnesia, calcium oxide, calcium hydroxide etc.
Among this embodiment, the alkali lye that is used for absorbing adopts ammoniacal liquor.
Described absorption liquid feed mechanism includes alkali liquid tank 15, alkali lye replenishment pump 16, circulation absorption pump I 11 and circulation absorption pump II 12.Described alkali liquid tank 15 is communicated with circulation absorption pump I 11 and circulation absorption pump II 12 by described alkali lye replenishment pump 16, makes ammoniacal liquor enter described first grade absorption tower and described two-level absorption tower, and replenishes because absorbing the ammoniacal liquor that sulfur dioxide consumes; The ammoniacal liquor that described alkali liquid tank 15 consumes is by out-of-bounds replenishing, and the fresh water (FW) that out-of-bounds provides is provided, with alkali lye dilution and control in the finite concentration scope.
The epimere absorber portion of described first grade absorption tower 8 and stage casing enriching section cut off by rising gas cap, and the described stage casing enriching section of first grade absorption tower 8 and hypomere liquid storage section are cut off by dividing plate; The bottom, described epimere absorption tower of first grade absorption tower 8 is communicated with described hypomere liquid storage section, the hypomere liquid storage section bottom of described first grade absorption tower 8 is communicated with circulation absorption pump I 11, shower in the epimere absorber portion of described circulation absorption pump I 11 and described first grade absorption tower 8 is communicated with, constitute the absorption liquid circulatory system of first grade absorption tower 8, enter the most of sulfur dioxide in the gas of first grade absorption tower 8 in order to absorption.
The epimere washing section of described two-level absorption tower 9 and hypomere absorber portion cut off by rising gas cap; Described circulation absorption pump II 12 is communicated with the hypomere absorber portion bottom of described two-level absorption tower 9, simultaneously, shower in the hypomere absorber portion of circulation absorption pump II 12 and described two-level absorption tower 9 is communicated with, constitute the absorption liquid circulatory system of two-level absorption tower 9, the residue sulfur dioxide that further will enter in the gas of two-level absorption tower 9 absorbs fully.
The epimere washing section bottom of described two-level absorption tower 9 is communicated with washing tank 13, shower in the epimere washing section of described washings circulating pump 14 and described two-level absorption tower 9 is communicated with, constitute the washings circulatory system, small amount of ammonia gas contained in the flue gas that enters two-level absorption tower 9 epimeres and ammonium sulfite are carried out spray washing; Described washing tank 13 is communicated with alkali liquid tank 15 in the absorbing and converting system by control valve, and the ammonia that the washing tank is 13 li and ammonium sulfite enter alkali liquid tank 15 adjusting ammonia concns after reaching finite concentration;
The hypomere liquid storage section bottom of described first grade absorption tower 8, the hypomere absorber portion bottom of two-level absorption tower 9 all are communicated with oxidation tank 18 by oxidation cycle pump 19, venturi-type eductors 17, constitute the sulfite oxidation system; After ammonium sulfite in the described absorption liquid reaches finite concentration, enter described sulfite oxidation system by control valve, after 19 pressurizations of oxidation cycle pump, enter oxidation tank 18 through venturi-type eductors 17, be oxidized to the ammonium sulfate slurries in the oxidation tank 18 with fully mixing to be incorporated in from described venturi-type eductors 17 inhaled airs;
Described oxidation tank 18 is communicated with shower in the enriching section of described first grade absorption tower stage casing by oxidation cycle pump 19; Simultaneously, being communicated with communicating pipe between oxidation cycle pump 19 and the exhanst gas outlet of described UTILIZATION OF VESIDUAL HEAT IN boiler 4, the described first grade absorption tower 8 stage casing enriching sections.
The enriching section bottom, stage casing of described first grade absorption tower 8 is communicated with serum pot 20, and makes described serum pot by the shower in the stage casing enriching section that concentrates circulating pump 21, control valve connection first grade absorption tower 8, constitutes slurries and concentrates the circulatory system.
The bottom of described serum pot 20 is communicated with Crystallization Separation system 23 by control valve, discharging pump 22, the mother liquor of described Crystallization Separation system 23 is communicated with serum pot 20, return serum pot 20 from Crystallization Separation system 23 isolated mother liquors, after the crystal drying system drying, the ammonium sulfate quality is up to state standards, send into packaging system, produce qualified ammonium sulfate product.
Shower in the absorber portion of the absorber portion of first grade absorption tower 8, enriching section and two-level absorption tower 9 is arranged to three layers, and the shower in the washing section of two-level absorption tower 9 is arranged to two-layer.
Fresh water (FW) enters washing tank 13 back and gets to two-level absorption tower epimere washing section top spray by washings circulating pump 14 and descend, return 13 pairs of flue gases of washing tank behind the washing flue gas and carry out circulation cleaning, the ammonia that the washing tank is 13 li and ammonium sulfite can enter alkali liquid tank 15 adjusting ammonia concns after reaching finite concentration.
It is combustion-supporting that the air one tunnel that is come by air blast 1 enters incinerator 3, and the temperature of UTILIZATION OF VESIDUAL HEAT IN boiler 4 outlet flue gases is regulated on another road; The saturated vapor that UTILIZATION OF VESIDUAL HEAT IN boiler 4 produces enter drum after decompressor 7 is regulated pressure can outside supply.
The ammoniacal liquor of described absorption liquid for being provided by alkali liquid tank 15; The ammoniacal liquor of alkali liquid tank 15 is squeezed into shower in the hypomere absorber portion of shower in the stage casing absorber portion of first grade absorption tower 8, two-level absorption tower 9 respectively after alkali lye replenishment pump 16 pressurization and through circulation absorption pump I 11 and circulation absorption pump II 12, the gas that is rich in sulfur dioxide is carried out absorption cleaning; The epimere absorber portion of first grade absorption tower 8 bottom absorption liquid import first grade absorption tower 8 hypomere liquid storage section, two-level absorption tower 9 hypomere absorber portion bottom and squeeze into the epimere absorber portion of first grade absorption tower 8, the hypomere absorber portion of two-level absorption tower 9 by circulation absorption pump I 11 and circulation absorption pump II 12 respectively, to the gas that the is rich in sulfur dioxide absorption cleaning that circulates; After ammonium sulfite in described first grade absorption tower 8 or described two-level absorption tower 9 absorption liquids reaches finite concentration, connect oxidation cycle pump 19 from the hypomere liquid storage section bottom of first grade absorption tower 8 or the bottom of two-level absorption tower 9 hypomere absorber portions by control valve, after 19 pressurizations of oxidation cycle pump, enter oxidation tank 18 through venturi-type eductors 17, fully mix to be incorporated in venturi-type eductors 17 inhaled airs and send into first grade absorption tower 8 stage casing enriching sections after being oxidized to ammonium sulfate in the oxidation tank 18, simultaneously, the exhanst gas outlet of oxidation cycle pump 19 and described UTILIZATION OF VESIDUAL HEAT IN boiler 4, communicating pipe between the described first grade absorption tower 8 stage casing enriching sections is communicated with; After ammonium sulfate reclaims fume afterheat, behind the hot flue gas heating evaporation that large quantity of moisture is come in by the bottom, form the ammonium sulfate slurries, described ammonium sulfate slurries flow into serum pot 20 from the enriching section bottom, stage casing of first grade absorption tower 8; Concentrate circulating pump 21 and squeeze into shower in the first grade absorption tower 8 stage casing enriching sections after the pressurization of the ammonium sulfate slurries in the serum pot 20, flow into serum pot 20 continuation circulation enrichments behind the hot flue gas heating evaporation that spray downwards, large quantity of moisture are come in by the bottom from the bottom; Ammonium sulfate slurries in the serum pot 20 reach capacity and send into Crystallization Separation system 23 by discharging pump, return serum pot 20 from Crystallization Separation system 23 isolated mother liquors, and after the crystal drying system drying, the ammonium sulfate quality is up to state standards, send into packaging system 25, produce qualified ammonium sulfate product.
The nitrogen 27 that connects described burner is to utilize its non-flammable character in air, before 2 igniting of described burner and flame-out and conversion system occur using when unusual, be used for guaranteeing the conversion system security of operation, stop security incident.
Reclaim controlling device and technology according to the described a kind of hydrogen sulfide containing chemical industry acid waste gas of embodiment 1, for reaching same purpose, Fig. 2, arrangement shown in Figure 3 can be arranged.
Fig. 2 with the difference of Fig. 1 is: first grade absorption tower 8 top exits are communicated with two-level absorption tower 9 after being communicated with booster fan 34 again; Two-level absorption tower 9 top exits are communicated with chimney 10 after being communicated with air-introduced machine 35 again.Purified gas adopts this connection when arranging multiplayer shower or gas pressure are low in the absorption tower, so that can be discharged smoothly by chimney.
Fig. 3 with the difference of Fig. 1 is: the exhanst gas outlet of the described UTILIZATION OF VESIDUAL HEAT IN boiler 4 of oxidation cycle pump 19 discord is communicated with communicating pipe with the stage casing enriching section of described first grade absorption tower 8, but being communicated with communicating pipe between the stage casing enriching section of the exhanst gas outlet of washings circulating pump 14 and described UTILIZATION OF VESIDUAL HEAT IN boiler 4 and described first grade absorption tower 8.
Claims (9)
1. a hydrogen sulfide containing chemical industry acid waste gas reclaims controlling device, it is characterized in that: described device includes air blast (1), burner (2), incinerator (3), UTILIZATION OF VESIDUAL HEAT IN boiler (4), drum (5), boiler feed pump (6), decompressor (7), first grade absorption tower (8), two-level absorption tower (9), washing tank (13), alkali liquid tank (15), oxidation tank (18), serum pot (20), Crystallization Separation system (23), drying system (24), packaging system (25) and all kinds of centrifugal pump;
Described air blast (1), burner (2), incinerator (3), UTILIZATION OF VESIDUAL HEAT IN boiler (4), drum (5), boiler feed pump (6), decompressor (7) constitute to be lighted, burns fully and be converted into the high-temperature gas that is rich in sulfur dioxide, high-temperature gas is lowered the temperature and reclaimed the conversion system of heat hydrogen sulfide containing acid waste gas;
Described boiler feed pump (6) is communicated with drum (5), decompressor (7), by the boiler water (26) that out-of-bounds replenishes after described boiler feed pump (6) pressurization, enter described UTILIZATION OF VESIDUAL HEAT IN boiler (4), boiler water in the UTILIZATION OF VESIDUAL HEAT IN boiler (4) absorbs the saturated vapor of the heat formation high pressure of described high-temperature gas, the output after decompressor (7) is regulated pressure of described saturated steam is out-of-bounds used for out-of-bounds installing;
The exhanst gas outlet of described UTILIZATION OF VESIDUAL HEAT IN boiler (4) is communicated with the stage casing enriching section of described first grade absorption tower (8), the cat head of described first grade absorption tower (8) is communicated with the hypomere absorber portion of described two-level absorption tower (9), and the cat head of described two-level absorption tower (9) is communicated with chimney (10);
Described first grade absorption tower (8), two-level absorption tower (9) and absorption liquid feed mechanism constitute the absorbing and converting system to the absorption cleaning that is rich in sulfur dioxide gas and generation sulphite;
Described absorption liquid feed mechanism includes alkali liquid tank (15), alkali lye replenishment pump (16), circulation absorption pump I (11) and circulation absorption pump II (12); Described alkali liquid tank (15) is communicated with circulation absorption pump I (11) and circulation absorption pump II (12) by described alkali lye replenishment pump (16), makes alkali lye enter described first grade absorption tower and two-level absorption tower; The alkali lye (32) that described alkali liquid tank (15) consumes is by out-of-bounds replenishing, and the fresh water (FW) (31) that out-of-bounds provides is provided, and alkali lye is diluted;
The epimere absorber portion of described first grade absorption tower and stage casing enriching section cut off by rising gas cap, and the described stage casing enriching section of first grade absorption tower and hypomere liquid storage section are cut off by dividing plate; The bottom, described epimere absorption tower of first grade absorption tower is communicated with by the pipeline in the first grade absorption tower outside with described hypomere liquid storage section, the hypomere liquid storage section bottom of described first grade absorption tower is communicated with circulation absorption pump I (11), shower in the epimere absorber portion of described circulation absorption pump I (11) and described first grade absorption tower is communicated with, constitute the absorption liquid circulatory system of first grade absorption tower, enter the most of sulfur dioxide in the gas of first grade absorption tower in order to absorption;
The epimere washing section bottom of described two-level absorption tower is communicated with washing tank (13), shower in the epimere washing section of washings circulating pump (14) and described two-level absorption tower is communicated with, constitute the washings circulatory system, a small amount of alkali lye contained in the flue gas that enters the two-level absorption tower epimere and sulphite are carried out spray washing;
The epimere washing section of described two-level absorption tower and hypomere absorber portion cut off by rising gas cap; Described circulation absorption pump II (12) is communicated with the hypomere absorber portion bottom of described two-level absorption tower, simultaneously, shower in the hypomere absorber portion of circulation absorption pump II (12) and described two-level absorption tower (9) is communicated with, and constitutes the absorption liquid circulatory system of two-level absorption tower;
Described washing tank (13) is communicated with alkali liquid tank (15) in the absorbing and converting system by control valve, and the alkali lye of washing tank (13) lining and sulphite enter alkali liquid tank (15) adjusting concentration of lye after reaching finite concentration;
The hypomere liquid storage section bottom of described first grade absorption tower, the hypomere absorber portion bottom of two-level absorption tower all are communicated with oxidation tank (18) by oxidation cycle pump (19), venturi-type eductors (17), constitute the sulfite oxidation system; After the sulphite of the absorption liquid in the described absorption liquid circulatory system reaches finite concentration, enter described sulfite oxidation system by control valve, after oxidation cycle pump (19) pressurization, enter oxidation tank (18) through venturi-type eductors (17), be oxidized to the sulfate slurries with fully mixing to be incorporated in the oxidation tank (18) from described venturi-type eductors (17) inhaled air (33);
Described oxidation tank (18) is communicated with shower in the enriching section of described first grade absorption tower stage casing by oxidation cycle pump (19);
The enriching section bottom, stage casing of described first grade absorption tower is communicated with serum pot (20), and makes described serum pot (20) by the shower in the stage casing enriching section that concentrates circulating pump (21), control valve connection first grade absorption tower, constitutes slurries and concentrates the circulatory system;
The bottom of described serum pot (20) is communicated with Crystallization Separation system (23) by control valve, discharging pump (22), the isolated mother liquor of described Crystallization Separation system (23) returns serum pot (20), after crystal drying system (24) drying, send into packaging system (25), produce sulfate product.
2. reclaim controlling device according to the described a kind of hydrogen sulfide containing chemical industry acid waste gas of claim 1, it is characterized in that: at needs UTILIZATION OF VESIDUAL HEAT IN boiler (4) when exit gas temperature is regulated, is drawn the temperature of one tunnel air conditioning UTILIZATION OF VESIDUAL HEAT IN boiler (4) outlet flue gas from air blast (1).
3. reclaim controlling device according to the described a kind of hydrogen sulfide containing chemical industry acid waste gas of claim 1, it is characterized in that: the exhanst gas outlet of described UTILIZATION OF VESIDUAL HEAT IN boiler (4) is communicated with communicating pipe and oxidation cycle pump (19) between the stage casing enriching section of described first grade absorption tower.
4. reclaim controlling device according to the described a kind of hydrogen sulfide containing chemical industry acid waste gas of claim 1, it is characterized in that: being communicated with communicating pipe between the exhanst gas outlet of washings circulating pump (14) and described UTILIZATION OF VESIDUAL HEAT IN boiler (4) and described first grade absorption tower (8) the stage casing enriching section.
5. reclaim controlling device according to the described a kind of hydrogen sulfide containing chemical industry acid waste gas of claim 1, it is characterized in that: washing section, the shower in the absorber portion of absorber portion, enriching section and the two-level absorption tower (9) of described first grade absorption tower (8) are one or more layers.
6. utilize the recovery of the recovery controlling device of the described a kind of hydrogen sulfide containing chemical industry acid waste gas of claim 1 to administer technology, it is characterized in that: will contain the chemical emission of hydrogen sulfide after burning, hydrogen sulfide is converted into sulfur dioxide, absorb through alkali lye again and be converted into sulphite, sulphite is sulfate through air oxidation, reclaim the chemical industry acid waste gas simultaneously and burn the heat formation saturated steam that produces, that is: auxiliary fuel gas (29) and instrument air (30) are after burner is lighted, feed the combustion air that hydrogen sulfide containing acid waste gas (28) and air blast (1) blast, in being rich in the incinerator of air (3), burn fully and be converted into the high-temperature gas that is rich in sulfur dioxide, after entering that UTILIZATION OF VESIDUAL HEAT IN boiler (4) reclaims a large amount of heats and regulating temperature by cold air, epimere absorber portion through entering first grade absorption tower (8) behind the enriching section recovery waste heat of the stage casing of first grade absorption tower (8) is sprayed after the absorption liquid that gets off sponges most of sulfur dioxide, discharge the hypomere absorber portion that enters two-level absorption tower (9) from cat head, sprayed after the absorption liquid that gets off further absorbs remaining sulfur dioxide fully by the hypomere absorber portion top of two-level absorption tower (9), enter the epimere washing section of two-level absorption tower, contained a small amount of alkali lye and sulphite spray the washings washing of getting off through the epimere washing section of two-level absorption tower in the flue gas, enter atmosphere from chimney (10) after demist;
The alkali lye of absorption liquid in described first grade absorption tower, the two-level absorption tower absorption liquid circulatory system for being provided by alkali liquid tank (15); The alkali lye (32) that alkali liquid tank (15) comes is squeezed into shower in the hypomere absorber portion of shower in first grade absorption tower (8) the epimere absorber portion, two-level absorption tower (9) respectively after alkali lye replenishment pump (16) pressurization and through circulation absorption pump I (11) and circulation absorption pump II (12), the gas that is rich in sulfur dioxide is carried out absorption cleaning; The absorption liquid of hypomere absorber portion bottom that imports absorption liquid, the two-level absorption tower of first grade absorption tower hypomere liquid storage section from the epimere absorber portion of first grade absorption tower bottom absorption liquid is squeezed into the epimere absorber portion of first grade absorption tower, the hypomere absorber portion of two-level absorption tower by circulation absorption pump I (11) and circulation absorption pump II (12) respectively, to the gas that the is rich in sulfur dioxide absorption cleaning that circulates; Sulphite in the described absorption liquid reaches finite concentration, at the bottom of tower, discharge by after oxidation cycle pump (19) pressurization, enter oxidation tank (18) through venturi-type eductors (17), be oxidized to sulfate in the oxidation tank with abundant mixed being incorporated in of venturi-type eductors (17) inhaled air (33), send into first grade absorption tower stage casing enriching section, the hot flue gas heating that sulfate liquor is come in by the bottom concentrates the back from the stage casing enriching section bottom inflow serum pot (20) of first grade absorption tower; Concentrate circulating pump (21) and squeeze into shower in the enriching section of first grade absorption tower stage casing after the pressurization of the slurries in the serum pot, flow into serum pot (20) from the bottom behind the hot flue gas heating evaporation that spray downwards, large quantity of moisture are come in by the bottom and continue the circulation enrichment; Sulfate slurries in the serum pot (20) reach capacity and send into Crystallization Separation system (23) by discharging pump (22), return serum pot (20) from the isolated mother liquor of Crystallization Separation system (23), after crystal drying system (24) drying, the sulfate quality is up to state standards, send into packaging system (25), produce qualified sulfate product.
7. administer technology according to the recovery of the described a kind of hydrogen sulfide containing chemical industry acid waste gas of claim 6, it is characterized in that: described washings enter the shower that washs in the epimere washing section of being got to two-level absorption tower (9) by washings circulating pump (14) in tank (13) back, washings spray downwards, return washing tank (13) behind the washing flue gas, flue gas is carried out circulation cleaning.
8. administer technology according to the recovery of the described a kind of hydrogen sulfide containing chemical industry acid waste gas of claim 6, it is characterized in that: the alkali lye of washing tank (13) lining and sulphite enter alkali liquid tank (15) adjusting concentration of lye after reaching finite concentration.
9. administer technology according to the recovery of claim 6 or 7 described a kind of hydrogen sulfide containing chemical industry acid waste gas, it is characterized in that: the sulfate in the oxidation tank (18) enters the communicating pipe between the stage casing enriching section of the exhanst gas outlet of UTILIZATION OF VESIDUAL HEAT IN boiler (4) and described first grade absorption tower, or washings enter the communicating pipe between the stage casing enriching section of the exhanst gas outlet of UTILIZATION OF VESIDUAL HEAT IN boiler (4) and described first grade absorption tower, the flue-gas temperature that enters described first grade absorption tower (8) in order to reduction by washings circulating pump (14).
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