CN103301732B - 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
- Publication number
- CN103301732B CN103301732B CN201310245931.3A CN201310245931A CN103301732B CN 103301732 B CN103301732 B CN 103301732B CN 201310245931 A CN201310245931 A CN 201310245931A CN 103301732 B CN103301732 B CN 103301732B
- Authority
- CN
- China
- Prior art keywords
- absorption tower
- pump
- gas
- grade
- communicated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Treating Waste Gases (AREA)
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 Treatment process field, relate generally to a kind of device and technique of hydrogen sulfide containing chemical industry sour gas recycling and administration, this device and process portion unit are applicable to the boiler smoke of high-load sulfur dioxide and the recycling and administration of chemical emission simultaneously.
Background technology
A lot of to the method for exhuast gas desulfurization hydrogen in chemical industry at present, the first kind is wet desulphurization.By the difference of desulfurizing agent, liquid absorption method can be divided into again and absorb oxidizing process two class.Liquid absorption method comprises and utilizes the chemical absorption method of alkaline solution, utilizes the Physical Absorption method of organic solvent and utilize the physical chemistry absorption process of Physical Absorption and chemical solvent simultaneously; Absorbing oxidizing process most popular is at present coordinate iron processes.These methods are generally equal can by-product sulphur, sulfuric acid or sulfate etc.
Equations of The Second Kind is dry desulfurization.Utilize reproducibility and the combustibility of hydrogen sulfide, carry out desulfurization with fixed oxygen agent or absorbent or directly burn.The 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 large, and desulfurizing agent needs super regeneration or replacing, and sulfur capacity is relatively low, is generally suitable for the meticulous desulfurization of gas.
What coal chemical industry produced is that main chemical industry sour gas mainly adopts claus process to carry out sulfur recovery improvement containing hydrogen sulfide, by the sour gas containing hydrogen sulfide in claus oven combustion, make partial vulcanization hydrogen-oxygen turn to sulfur dioxide, sulfur dioxide reacts generation sulphur on a catalyst with remaining unreacted hydrogen sulfide again.But in this technique, in unstripped gas, the too low meeting of concentration of hydrogen sulfide causes device normally to run, and cannot meet the needs of long-period safety production, and complicated operation, occupation area of equipment is large, 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 recycling and administration device and technique.
The present invention takes following technical scheme to complete its invention task:
A kind of hydrogen sulfide containing chemical industry acid waste gas recycling and administration device, described device includes air blast, burner, incinerator, Waste-heat boiler, drum, decompressor, first grade absorption tower, two-level absorption tower, type washing trough, 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, Waste-heat boiler, drum, decompressor form hydrogen sulfide containing acid waste gas is lighted, burn completely and be converted into be rich in sulfur dioxide high-temperature gas, high-temperature gas lowered the temperature and reclaims the conversion system of heat;
Described boiler feed pump is communicated with drum, decompressor, by the boiler water out-of-bounds supplemented after described boiler feed pump pressurizes, enter described Waste-heat boiler, boiler water in Waste-heat boiler absorbs the saturated vapor of the heat formation high pressure of described high-temperature gas, described saturated steam regulates after pressure through decompressor and exports out-of-bounds, for out-of-bounds device;
The exhanst gas outlet of described Waste-heat boiler is communicated with the stage casing enriching section of described first grade absorption tower, and the tower top of described first grade absorption tower is communicated with the hypomere absorber portion of described two-level absorption tower, and the tower top of described two-level absorption tower is communicated with chimney;
Described first grade absorption tower, two-level absorption tower and absorbing liquid feed mechanism form being rich in the absorption cleaning of sulfur dioxide gas and generating the absorbing and converting system of sulphite;
Described absorbing liquid feed mechanism includes alkali liquid tank, alkali lye replenishment pump, cyclic absorption pump I and cyclic absorption pump II; Described alkali liquid tank is communicated with cyclic absorption pump II with cyclic absorption pump I by described alkali lye replenishment pump, makes alkali lye enter described first grade absorption tower, described two-level absorption tower, and supplements the alkali lye consumed because of sulfur dioxide absorption; The alkali lye of described alkali liquid tank consumption by out-of-bounds supplementing, and adds the fresh water (FW) out-of-bounds provided, and is diluted by alkali lye and controls within the scope of finite concentration;
The epimere absorber portion of described first grade absorption tower and stage casing enriching section cut off by rising gas cap, and described stage casing enriching section and the hypomere liquid storage section of first grade absorption tower are cut off by dividing plate; Bottom the described epimere absorption tower of first grade absorption tower with described hypomere liquid storage section by the pipeline communication in first grade absorption tower outside, be communicated with cyclic absorption pump I bottom the hypomere liquid storage section of described first grade absorption tower, described cyclic absorption pump I is communicated with the shower in the epimere absorber portion of described first grade absorption tower, form the absorbing liquid circulatory system of first grade absorption tower, in order to absorb the most of sulfur dioxide entered in the gas of first grade absorption tower;
The epimere washing section of described two-level absorption tower and hypomere absorber portion cut off by rising gas cap; Described cyclic absorption pump II is communicated with bottom the hypomere absorber portion of described two-level absorption tower, simultaneously, cyclic absorption pump II is communicated with the shower in the hypomere absorber portion of described two-level absorption tower, form the absorbing liquid circulatory system of two-level absorption tower, further the residue sulfur dioxide entered in the gas of two-level absorption tower is absorbed completely;
Be communicated with type washing trough bottom the epimere washing section of described two-level absorption tower, described washings circulating pump is communicated with the shower in the epimere washing section of described two-level absorption tower, form washing water circulation system, spray washing is carried out to a small amount of alkali lye contained in the flue gas entering two-level absorption tower epimere and sulphite;
Described type washing trough is communicated with alkali liquid tank in absorbing and converting system by control valve, and the alkali lye in type washing trough and sulphite enter alkali liquid tank and regulates concentration of lye after reaching finite concentration;
Bottom the hypomere liquid storage section of described first grade absorption tower, be all communicated with oxidation tank by oxidation cycle pump, venturi-type eductors bottom the hypomere absorber portion of two-level absorption tower, form sulfite oxidation system; After the sulphite of the absorbing liquid in the described absorbing liquid circulatory system reaches finite concentration, described sulfite oxidation system is entered by control valve, after being pressurizeed by oxidation cycle pump, enter oxidation tank through venturi-type eductors, fully mix to be incorporated in oxidation tank being oxidized to sulfate slurries with the air sucked from described venturi-type eductors;
Described oxidation tank is communicated with the shower in described first order absorption midsection enriching section by oxidation cycle pump;
Be communicated with serum pot bottom the stage casing enriching section of described first grade absorption tower, and make described serum pot by the shower in the stage casing enriching section of concentration cycles pump, control valve connection first grade absorption tower, form slurries concentration cycles system;
The bottom of described serum pot is by control valve, discharging pump and Crystallization Separation system connectivity, and the mother liquor that described Crystallization Separation systematic position goes out returns serum pot, after the drying of crystal drying system, sends into packaging system, produces sulfate product.
Be provided with air blast in described conversion system, it is combustion-supporting that the air come by air blast enters incinerator, when needs Waste-heat boiler exit gas temperature is lower, can draw the temperature of a road air conditioning Waste-heat boiler exiting flue gas again from air blast.
Shower in the washing section of the absorber portion of described first grade absorption tower, enriching section and two-level absorption tower, absorber portion can be arranged to one or more layers.
Utilize the recycling and administration technique of the recycling and administration device of above-mentioned hydrogen sulfide containing chemical industry acid waste gas, by the chemical emission containing hydrogen sulfide after burning, hydrogen sulfide is converted into sulfur dioxide, sulphite is converted into again through alkali liquor absorption, sulphite is sulfate through air oxidation, reclaim chemical industry acid waste gas simultaneously and burn the heat formation saturated steam produced, that is: auxiliary fuel gas and instrument air are after burner is lighted, pass into the combustion air that hydrogen sulfide containing acid waste gas and air blast blast, burn completely in the aeriferous incinerator of richness and be converted into the high-temperature gas being rich in sulfur dioxide, enter Waste-heat boiler reclaim amount of heat and regulated after temperature by cold air, the epimere absorber portion entering first grade absorption tower after the stage casing enriching section recovery waste heat of first grade absorption tower is sprayed after the absorbing liquid got off sponges most of sulfur dioxide, the hypomere absorber portion entering two-level absorption tower is discharged from tower top, after further remaining sulfur dioxide being absorbed completely by the absorbing liquid that the hypomere absorber portion top of two-level absorption tower sprays, enter the epimere washing section of two-level absorption tower, the washings that a small amount of alkali lye contained in flue gas and sulphite sprays through the epimere washing section of two-level absorption tower wash, air is entered from chimney after demist.
Described alkali lye can be one or more chemical substances water-soluble or with water generation chemical reaction after formed in alkalescence solution, described chemical substance can be liquefied ammonia, ammoniacal liquor, NaOH, sodium carbonate, magnesia, calcium oxide, calcium hydroxide etc.Different alkaline solution absorption sulfur dioxide after air oxidation, formation be corresponding sulfate, during as used liquefied ammonia, ammoniacal liquor, form ammonium sulfate; When using NaOH, sodium carbonate, form sodium sulphate; When using calcium oxide, calcium hydroxide, form calcium sulfate.
Got to the shower in the epimere washing section of two-level absorption tower after fresh water (FW) enters type washing trough by washings circulating pump, washings spray downwards, return type washing trough, carry out circulation cleaning to flue gas after washing flue gas.Alkali lye in type washing trough and sulphite enter alkali liquid tank and regulate concentration of lye after reaching finite concentration.
The alkali lye of absorbing liquid for being provided by alkali liquid tank in described first grade absorption tower, the two-level absorption tower absorbing liquid circulatory system; The alkali lye that alkali liquid tank comes after the pressurization of alkali lye replenishment pump and the shower squeezed into respectively through cyclic absorption pump I and cyclic absorption pump II in the hypomere absorber portion of shower in first grade absorption tower epimere absorber portion, two-level absorption tower, carries out absorption cleaning to the gas being rich in sulfur dioxide; Squeeze into the epimere absorber portion of first grade absorption tower, the hypomere absorber portion of two-level absorption tower respectively by cyclic absorption pump I and cyclic absorption pump II bottom the hypomere absorber portion that bottom the epimere absorber portion of first grade absorption tower, absorbing liquid imports the hypomere liquid storage section of first grade absorption tower, two-level absorption tower, cyclic absorption purification is carried out to the gas being rich in sulfur dioxide; Sulphite in described absorbing liquid reaches finite concentration, discharge after being pressurizeed by oxidation cycle pump at the bottom of tower, oxidation tank is entered through venturi-type eductors, the air sucked with venturi-type eductors fully mixed being incorporated in oxidation tank is oxidized to sulfate, send into the shower of first order absorption midsection enriching section, sulfate liquor flows into serum pot after being concentrated by the heat smoke heating come in bottom bottom the stage casing enriching section of first grade absorption tower; Concentration cycles pump squeezes into shower in first order absorption midsection enriching section after the slurries pressurization in serum pot, sprays downwards, and after the heat smoke heating evaporation that large quantity of moisture is come in by bottom, slurries flow into serum pot and continue circulation enrichment from bottom; Crystallization Separation system is sent into through discharging pump after sulfate slurries in serum pot reach capacity, the mother liquor gone out from Crystallization Separation systematic position returns serum pot, and after the drying of crystal drying system, sulfate quality is up to state standards, send into packaging system, produce qualified sulfate product.
The one hydrogen sulfide containing chemical industry acid waste gas recycling and administration device that the present invention proposes and technique, take technique scheme hydrogen sulfide containing chemical emission can be converted into valuable sulfate product, reclaim chemical emission and burned the heat produced, reach the object of administering waste gas and heat recovery simultaneously.
Accompanying drawing explanation
Accompanying drawing 1 is device of the present invention and process chart.
Accompanying drawing 2, accompanying drawing 3 are respectively embodiment 2, the device of embodiment 3 and process chart.
In figure: 1, air blast, 2, burner, 3, incinerator, 4, Waste-heat boiler, 5, drum, 6, boiler feed pump, 7, decompressor, 8, first grade absorption tower, 9, two-level absorption tower, 10, chimney, 11, cyclic absorption pump I, 12, cyclic absorption pump II, 13, type washing trough, 14, washings circulating pump, 15, alkali liquid tank, 16, alkali lye replenishment pump, 17, venturi-type eductors, 18, oxidation tank, 19, oxidation cycle pump, 20, serum pot, 21, concentration cycles pump, 22, discharging pump, 23, Crystallization Separation system, 24, drying system, 25, packaging system, 26, boiler water, 27, nitrogen, 28, sulfide hydrogen acid waste gas, 29, auxiliary fuel gas, 30, instrument air, 31, fresh water (FW), 32, alkali lye, 33, air.
Detailed description of the invention
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 recycling and administration device and technique, described device includes air blast 1, burner 2, incinerator 3, Waste-heat boiler 4, drum 5, first grade absorption tower 8, two-level absorption tower 9, type washing trough 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, Waste-heat boiler 4, drum 5, boiler feed pump 6, decompressor 7 form hydrogen sulfide containing acid waste gas is lighted, burn completely and be converted into be rich in sulfur dioxide high-temperature gas, high-temperature gas lowered the temperature and reclaims the conversion system of heat.
Described boiler feed pump 6 is communicated with drum 5, decompressor 7, by the boiler water 26 out-of-bounds supplemented after described boiler feed pump 6 pressurizes, enters described Waste-heat boiler 4.The heat that boiler water in Waste-heat boiler 4 absorbs described high-temperature gas forms the saturated vapor of high pressure, and described saturated steam regulates after pressure through decompressor 7 and exports out-of-bounds, for out-of-bounds device.
The exhanst gas outlet of described Waste-heat boiler 4 is communicated with the stage casing enriching section of described first grade absorption tower 8, and the tower top of described first grade absorption tower 8 is communicated with the hypomere absorber portion of described two-level absorption tower 9, and the tower top of described two-level absorption tower 9 is communicated with chimney 10.
Described first grade absorption tower 8, two-level absorption tower 9 and absorbing liquid feed mechanism are formed being rich in the absorption cleaning of sulfur dioxide gas and generating the absorbing and converting system of sulphite.
Described absorbing liquid is alkaline solution, can be one or more chemical substances water-soluble or with water generation chemical reaction after formed in alkalescence solution, described chemical substance can be liquefied ammonia, ammoniacal liquor, NaOH, sodium carbonate, magnesia, calcium oxide, calcium hydroxide etc.
In this embodiment, adopt ammoniacal liquor for the alkali lye absorbed.
Described absorbing liquid feed mechanism includes alkali liquid tank 15, alkali lye replenishment pump 16, cyclic absorption pump I 11 and cyclic absorption pump II 12.Described alkali liquid tank 15 is communicated with cyclic absorption pump II 12 with cyclic absorption pump I 11 by described alkali lye replenishment pump 16, makes ammoniacal liquor enter described first grade absorption tower and described two-level absorption tower, and supplements the ammoniacal liquor consumed because of sulfur dioxide absorption; The ammoniacal liquor that described alkali liquid tank 15 consumes by out-of-bounds supplementing, and adds the fresh water (FW) out-of-bounds provided, and is diluted by alkali lye and controls within the scope of finite concentration.
The epimere absorber portion of described first grade absorption tower 8 and stage casing enriching section cut off by rising gas cap, and described stage casing enriching section and the hypomere liquid storage section of first grade absorption tower 8 are cut off by dividing plate; Be communicated with described hypomere liquid storage section bottom the described epimere absorption tower of first grade absorption tower 8, be communicated with cyclic absorption pump I 11 bottom the hypomere liquid storage section of described first grade absorption tower 8, described cyclic absorption pump I 11 is communicated with the shower in the epimere absorber portion of described first grade absorption tower 8, form the absorbing liquid circulatory system of first grade absorption tower 8, in order to absorb the most of sulfur dioxide entered in the gas of first grade absorption tower 8.
The epimere washing section of described two-level absorption tower 9 and hypomere absorber portion cut off by rising gas cap; Described cyclic absorption pump II 12 is communicated with bottom the hypomere absorber portion of described two-level absorption tower 9, simultaneously, cyclic absorption pump II 12 is communicated with the shower in the hypomere absorber portion of described two-level absorption tower 9, form the absorbing liquid circulatory system of two-level absorption tower 9, further the residue sulfur dioxide entered in the gas of two-level absorption tower 9 is absorbed completely.
Be communicated with type washing trough 13 bottom the epimere washing section of described two-level absorption tower 9, described washings circulating pump 14 is communicated with the shower in the epimere washing section of described two-level absorption tower 9, form washing water circulation system, spray washing is carried out to a small amount of ammonia contained in the flue gas entering two-level absorption tower 9 epimere and ammonium sulfite; Described type washing trough 13 is communicated with alkali liquid tank in absorbing and converting system 15 by control valve, and the ammonia that type washing trough is 13 li and ammonium sulfite enter alkali liquid tank 15 and regulate ammonia concn after reaching finite concentration;
Bottom the hypomere liquid storage section of described first grade absorption tower 8, be all communicated with oxidation tank 18 by oxidation cycle pump 19, venturi-type eductors 17 bottom the hypomere absorber portion of two-level absorption tower 9, form sulfite oxidation system; After ammonium sulfite in described absorbing liquid reaches finite concentration, described sulfite oxidation system is entered by control valve, after being pressurizeed by oxidation cycle pump 19, enter oxidation tank 18 through venturi-type eductors 17, fully mix to be incorporated in oxidation tank 18 being oxidized to ammonium sulfate slurries with the air sucked from described venturi-type eductors 17;
Described oxidation tank 18 is communicated with the shower in described first order absorption midsection enriching section by oxidation cycle pump 19; Meanwhile, being communicated with communicating pipe between the exhanst gas outlet of oxidation cycle pump 19 and described Waste-heat boiler 4, described first grade absorption tower 8 stage casing enriching section.
Be communicated with serum pot 20 bottom the stage casing enriching section of described first grade absorption tower 8, and make described serum pot by the shower in the stage casing enriching section of concentration cycles pump 21, control valve connection first grade absorption tower 8, form slurries concentration cycles 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, serum pot 20 is returned from the isolated mother liquor of Crystallization Separation system 23, after the drying of crystal drying system, ammonium sulfate quality is up to state standards, send into packaging system, produce qualified ammonium sulfate product.
Auxiliary fuel gas 29 and instrument air 30 are after burner 2 is lighted, pass into the combustion air that hydrogen sulfide containing acid waste gas 28 blasts with air blast 1, burn completely in the aeriferous incinerator of richness and be converted into the high-temperature gas being rich in sulfur dioxide, enter Waste-heat boiler 4 and reclaim amount of heat, temperature (air blast 1 blasts another road of air for regulating cooling to the high-temperature gas of Waste-heat boiler 4) is regulated by cold air, after the stage casing enriching section recovery waste heat of first grade absorption tower 8, enter after epimere absorber portion sponged most of sulfur dioxide by the absorbing liquid sprayed from top, the hypomere absorber portion entering two-level absorption tower 9 is discharged from tower top, after remaining sulfur dioxide absorbs by circulating absorption solution that absorber portion top sprays further completely, enter two-level absorption tower 9 epimere washing section, the washings washing that flue gas containing a small amount of ammonia and ammonium sulfite sprays through washing section top, air is entered from chimney 10 after demist, the pollution that the aerosol avoiding the escaping of ammonia and formation carries out air.
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.
After fresh water (FW) enters type washing trough 13 by washings circulating pump 14 get to two-level absorption tower epimere washing section top spray and under, return type washing trough 13 pairs of flue gases after washing flue gas and carry out circulation cleaning, alkali liquid tank 15 can be entered after the ammonia that type washing trough is 13 li and ammonium sulfite reach finite concentration and regulate ammonia concn.
It is combustion-supporting that air one tunnel come by air blast 1 enters incinerator 3, and another road regulates the temperature of Waste-heat boiler 4 exiting flue gas; The saturated vapor that Waste-heat boiler 4 produces enters drum and regulates after pressure can supply outward through decompressor 7.
The ammoniacal liquor of described absorbing liquid for being provided by alkali liquid tank 15, the ammoniacal liquor of alkali liquid tank 15 after alkali lye replenishment pump 16 pressurizes and the shower squeezed into respectively through cyclic absorption pump I 11 and cyclic absorption pump II 12 in the hypomere absorber portion of shower in the stage casing absorber portion of first grade absorption tower 8, two-level absorption tower 9, carries out absorption cleaning to the gas being rich in sulfur dioxide, squeeze into the epimere absorber portion of first grade absorption tower 8, the hypomere absorber portion of two-level absorption tower 9 respectively by cyclic absorption pump I 11 and cyclic absorption pump II 12 bottom the hypomere absorber portion that bottom the epimere absorber portion of first grade absorption tower 8, absorbing liquid imports the hypomere liquid storage section of first grade absorption tower 8, two-level absorption tower 9, cyclic absorption purification is carried out to the gas being rich in sulfur dioxide, after ammonium sulfite in described first grade absorption tower 8 or described two-level absorption tower 9 absorbing liquid reaches finite concentration, bottom the hypomere liquid storage section of first grade absorption tower 8 or the bottom of two-level absorption tower 9 hypomere absorber portion connect oxidation cycle pump 19 by control valve, after being pressurizeed by oxidation cycle pump 19, oxidation tank 18 is entered through venturi-type eductors 17, the air sucked with venturi-type eductors 17 is fully mixed be incorporated in be oxidized to ammonium sulfate in oxidation tank 18 after send into first grade absorption tower 8 stage casing enriching section, simultaneously, the exhanst gas outlet of oxidation cycle pump 19 and described Waste-heat boiler 4, communicating pipe between the enriching section of described first grade absorption tower 8 stage casing is communicated with, after ammonium sulfate Mist heat recovering, after the heat smoke heating evaporation that large quantity of moisture is come in by bottom, form ammonium sulfate slurries, described ammonium sulfate slurries flow into serum pot 20 bottom the stage casing enriching section of first grade absorption tower 8, concentration cycles pump 21 squeezes into shower in the enriching section of first grade absorption tower 8 stage casing after the ammonium sulfate slurries pressurization in serum pot 20, sprays downwards, flows into serum pot 20 continue circulation enrichment after the heat smoke heating evaporation that large quantity of moisture is come in by bottom from bottom, Crystallization Separation system 23 is sent into through discharging pump after ammonium sulfate slurries in serum pot 20 reach capacity, serum pot 20 is returned from the isolated mother liquor of Crystallization Separation system 23, and after the drying of crystal drying system, ammonium sulfate quality is up to state standards, send into packaging system 25, produce qualified ammonium sulfate product.
The nitrogen 27 connecting described burner utilizes its non-flammable character in atmosphere, using, for ensureing conversion system security of operation, stopping security incident when there is exception with flame-out and conversion system before described burner 2 is lighted a fire.
According to the one hydrogen sulfide containing chemical industry acid waste gas recycling and administration device described in embodiment 1 and technique, for reaching same object, the arrangement shown in Fig. 2, Fig. 3 can be had.
The difference of Fig. 2 and Fig. 1 is: first grade absorption tower 8 top exit is communicated with two-level absorption tower 9 after being communicated with booster fan 34 again; Two-level absorption tower 9 top exit is communicated with chimney 10 after being communicated with air-introduced machine 35 again.In absorption tower arranging multiplayer shower or gas pressure low time adopt this connection, discharged smoothly by chimney to enable purified gas.
The difference of Fig. 3 and Fig. 1 is: oxidation cycle pump 19 is got along well being communicated with communicating pipe of the exhanst gas outlet of described Waste-heat boiler 4 and the stage casing enriching section of described first grade absorption tower 8, but being communicated with communicating pipe between the exhanst gas outlet of washings circulating pump 14 and described Waste-heat boiler 4 and the stage casing enriching section of described first grade absorption tower 8.
Claims (9)
1. a hydrogen sulfide containing chemical industry acid waste gas recycling and administration device, is characterized in that: described device includes air blast (1), burner (2), incinerator (3), Waste-heat boiler (4), drum (5), boiler feed pump (6), decompressor (7), first grade absorption tower (8), two-level absorption tower (9), type washing trough (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), Waste-heat boiler (4), drum (5), boiler feed pump (6), decompressor (7) form hydrogen sulfide containing acid waste gas is lighted, burn completely and be converted into be rich in sulfur dioxide high-temperature gas, high-temperature gas lowered the temperature and reclaims the conversion system of heat;
Described boiler feed pump (6) is communicated with drum (5), decompressor (7), by the boiler water out-of-bounds supplemented (26) after described boiler feed pump (6) pressurizes, enter described Waste-heat boiler (4), boiler water in Waste-heat boiler (4) absorbs the saturated vapor of the heat formation high pressure of described high-temperature gas, described saturated steam regulates after pressure through decompressor (7) and exports out-of-bounds, for out-of-bounds device;
The exhanst gas outlet of described Waste-heat boiler (4) is communicated with the stage casing enriching section of described first grade absorption tower (8), the tower top of described first grade absorption tower (8) is communicated with the hypomere absorber portion of described two-level absorption tower (9), and the tower top of described two-level absorption tower (9) is communicated with chimney (10);
Described first grade absorption tower (8), two-level absorption tower (9) and absorbing liquid feed mechanism form being rich in the absorption cleaning of sulfur dioxide gas and generating the absorbing and converting system of sulphite;
Described absorbing liquid feed mechanism includes alkali liquid tank (15), alkali lye replenishment pump (16), cyclic absorption pump I (11) and cyclic absorption pump II (12); Described alkali liquid tank (15) is communicated with cyclic absorption pump II (12) with cyclic absorption pump I (11) 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 by out-of-bounds supplementing, and adds the fresh water (FW) (31) out-of-bounds provided, and is diluted by alkali lye;
The epimere absorber portion of described first grade absorption tower and stage casing enriching section cut off by rising gas cap, and described stage casing enriching section and the hypomere liquid storage section of first grade absorption tower are cut off by dividing plate; Bottom the described epimere absorption tower of first grade absorption tower with described hypomere liquid storage section by the pipeline communication in first grade absorption tower outside, be communicated with cyclic absorption pump I (11) bottom the hypomere liquid storage section of described first grade absorption tower, described cyclic absorption pump I (11) is communicated with the shower in the epimere absorber portion of described first grade absorption tower, form the absorbing liquid circulatory system of first grade absorption tower, in order to absorb the most of sulfur dioxide entered in the gas of first grade absorption tower;
Be communicated with type washing trough (13) bottom the epimere washing section of described two-level absorption tower, washings circulating pump (14) is communicated with the shower in the epimere washing section of described two-level absorption tower, form washing water circulation system, spray washing is carried out to a small amount of alkali lye contained in the flue gas entering two-level absorption tower epimere and sulphite;
The epimere washing section of described two-level absorption tower and hypomere absorber portion cut off by rising gas cap; Described cyclic absorption pump II (12) is communicated with bottom the hypomere absorber portion of described two-level absorption tower, simultaneously, cyclic absorption pump II (12) is communicated with the shower in the hypomere absorber portion of described two-level absorption tower (9), forms the absorbing liquid circulatory system of two-level absorption tower;
Described type washing trough (13) is communicated with alkali liquid tank in absorbing and converting system (15) by control valve, enters alkali liquid tank (15) and regulate concentration of lye after the alkali lye that type washing trough (13) is inner and sulphite reach finite concentration;
Bottom the hypomere liquid storage section of described first grade absorption tower, be all communicated with oxidation tank (18) by oxidation cycle pump (19), venturi-type eductors (17) bottom the hypomere absorber portion of two-level absorption tower, form sulfite oxidation system; After the sulphite of the absorbing liquid in the described absorbing liquid circulatory system reaches finite concentration, described sulfite oxidation system is entered by control valve, after being pressurizeed by oxidation cycle pump (19), enter oxidation tank (18) through venturi-type eductors (17), fully mix to be incorporated in oxidation tank (18) being oxidized to sulfate slurries with the air (33) sucked from described venturi-type eductors (17);
Described oxidation tank (18) is communicated with the shower in described first order absorption midsection enriching section by oxidation cycle pump (19);
Be communicated with serum pot (20) bottom the stage casing enriching section of described first grade absorption tower, and make described serum pot (20) by the shower in the stage casing enriching section of concentration cycles pump (21), control valve connection first grade absorption tower, form slurries concentration cycles 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. according to one according to claim 1 hydrogen sulfide containing chemical industry acid waste gas recycling and administration device, it is characterized in that: when needs regulate Waste-heat boiler (4) exit gas temperature, draw the temperature of road air conditioning Waste-heat boiler (4) exiting flue gas from air blast (1).
3., according to one according to claim 1 hydrogen sulfide containing chemical industry acid waste gas recycling and administration device, it is characterized in that: the communicating pipe between the exhanst gas outlet of described Waste-heat boiler (4) and the stage casing enriching section of described first grade absorption tower is communicated with oxidation cycle pump (19).
4. according to one according to claim 1 hydrogen sulfide containing chemical industry acid waste gas recycling and administration device, it is characterized in that: being communicated with communicating pipe between the exhanst gas outlet of washings circulating pump (14) and described Waste-heat boiler (4) and described first grade absorption tower (8) stage casing enriching section.
5. according to one according to claim 1 hydrogen sulfide containing chemical industry acid waste gas recycling and administration device, it is characterized in that: the shower in the washing section of the absorber portion of described first grade absorption tower (8), enriching section and two-level absorption tower (9), absorber portion is one or more layers.
6. utilize the recycling and administration technique of the recycling and administration device of a kind of hydrogen sulfide containing chemical industry acid waste gas described in claim 1, it is characterized in that: by the chemical emission containing hydrogen sulfide after burning, hydrogen sulfide is converted into sulfur dioxide, sulphite is converted into again through alkali liquor absorption, sulphite is sulfate through air oxidation, reclaim chemical industry acid waste gas simultaneously and burn the heat formation saturated steam produced, that is: auxiliary fuel gas (29) and instrument air (30) are after burner is lighted, pass into the combustion air that hydrogen sulfide containing acid waste gas (28) blasts with air blast (1), burn completely in the aeriferous incinerator of richness (3) and be converted into the high-temperature gas being rich in sulfur dioxide, enter Waste-heat boiler (4) reclaim amount of heat and regulated after temperature by cold air, the epimere absorber portion entering first grade absorption tower (8) after the stage casing enriching section recovery waste heat of first grade absorption tower (8) is sprayed after the absorbing liquid got off sponges most of sulfur dioxide, the hypomere absorber portion entering two-level absorption tower (9) is discharged from tower top, after further remaining sulfur dioxide being absorbed completely by the absorbing liquid that the hypomere absorber portion top of two-level absorption tower (9) sprays, enter the epimere washing section of two-level absorption tower, the washings that a small amount of alkali lye contained in flue gas and sulphite sprays through the epimere washing section of two-level absorption tower wash, air is entered from chimney (10) after demist,
Absorbing liquid in described first grade absorption tower, the two-level absorption tower absorbing liquid circulatory system is the alkali lye provided by alkali liquid tank (15); The alkali lye (32) that alkali liquid tank (15) comes after alkali lye replenishment pump (16) pressurization and the shower squeezed into respectively through cyclic absorption pump I (11) and cyclic absorption pump II (12) in the hypomere absorber portion of shower in first grade absorption tower (8) epimere absorber portion, two-level absorption tower (9), carries out absorption cleaning to the gas being rich in sulfur dioxide; Absorbing liquid bottom the hypomere absorber portion that absorbing liquid imports the absorbing liquid of first grade absorption tower hypomere liquid storage section, two-level absorption tower bottom the epimere absorber portion of first grade absorption tower squeezes into the epimere absorber portion of first grade absorption tower, the hypomere absorber portion of two-level absorption tower respectively by cyclic absorption pump I (11) and cyclic absorption pump II (12), carries out cyclic absorption purification to the gas being rich in sulfur dioxide; Sulphite in described absorbing liquid reaches finite concentration, discharge after being pressurizeed by oxidation cycle pump (19) at the bottom of tower, oxidation tank (18) is entered through venturi-type eductors (17), the air (33) sucked with venturi-type eductors (17) fully mixed being incorporated in oxidation tank is oxidized to sulfate, send into first order absorption midsection enriching section, sulfate liquor flows into serum pot (20) after being concentrated by the heat smoke heating come in bottom bottom the stage casing enriching section of first grade absorption tower; Concentration cycles pump (21) squeezes into shower in first order absorption midsection enriching section after the slurries pressurization in serum pot, sprays downwards, flows into serum pot (20) continue circulation enrichment after the heat smoke heating evaporation that large quantity of moisture is come in by bottom from bottom; Crystallization Separation system (23) is sent into through discharging pump (22) after sulfate slurries in serum pot (20) reach capacity, serum pot (20) is returned from Crystallization Separation system (23) isolated mother liquor, after crystal drying system (24) drying, sulfate quality is up to state standards, send into packaging system (25), produce qualified sulfate product.
7. according to recycling and administration technique according to claim 6, it is characterized in that: after described washings enter type washing trough (13), got to the shower in the epimere washing section of two-level absorption tower (9) by washings circulating pump (14), washings spray downwards, return type washing trough (13) after washing flue gas, circulation cleaning is carried out to flue gas.
8. according to recycling and administration technique according to claim 6, it is characterized in that: enter alkali liquid tank (15) after the alkali lye that type washing trough (13) is inner and sulphite reach finite concentration and regulate concentration of lye.
9. according to the recycling and administration technique described in claim 6 or 7, it is characterized in that: the sulfate in oxidation tank (18) enters the communicating pipe between the exhanst gas outlet of Waste-heat boiler (4) and the stage casing enriching section of described first grade absorption tower, or washings enter the communicating pipe between the exhanst gas outlet of Waste-heat boiler (4) and the stage casing enriching section of described first grade absorption tower by washings circulating pump (14), in order to reduce the flue-gas temperature entering described first grade absorption tower (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310245931.3A CN103301732B (en) | 2013-06-20 | 2013-06-20 | Device and process for recycling and treating hydrogen sulfide-containing chemical acid waste gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310245931.3A CN103301732B (en) | 2013-06-20 | 2013-06-20 | Device and process for recycling and treating hydrogen sulfide-containing chemical acid waste gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103301732A CN103301732A (en) | 2013-09-18 |
| CN103301732B true CN103301732B (en) | 2015-01-21 |
Family
ID=49127709
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310245931.3A Expired - Fee Related CN103301732B (en) | 2013-06-20 | 2013-06-20 | Device and process for recycling and treating hydrogen sulfide-containing chemical acid waste gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103301732B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10016721B1 (en) | 2017-05-25 | 2018-07-10 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desufurization process and apparatus |
| US10092877B1 (en) | 2017-05-25 | 2018-10-09 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10099170B1 (en) | 2017-06-14 | 2018-10-16 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US10112145B1 (en) | 2017-09-07 | 2018-10-30 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
| US20190001267A1 (en) | 2017-07-03 | 2019-01-03 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10207220B2 (en) | 2017-03-15 | 2019-02-19 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103721553A (en) * | 2014-01-07 | 2014-04-16 | 江苏新世纪江南环保股份有限公司 | Method for efficiently removing acid gas sulfide by ammonia process desulfurization technique |
| CN103939918B (en) * | 2014-04-11 | 2017-01-25 | 江苏新世纪江南环保股份有限公司 | Incineration method for acid gas and liquid purification |
| CN104031709A (en) * | 2014-05-26 | 2014-09-10 | 沈阳航空航天大学 | Methane micro-aerobic wet-type ammonia desulphurization device |
| CN105020723A (en) * | 2015-07-30 | 2015-11-04 | 中国五环工程有限公司 | Low-sulfur-discharge sulfur recovering technique and system based on Claus reaction system |
| CN108786397A (en) * | 2017-04-28 | 2018-11-13 | 湖南中天元环境工程有限公司 | A kind of processing method and system of Claus device exhausts |
| CN108046544B (en) * | 2018-01-25 | 2020-09-11 | 轻工业环境保护研究所 | Sulfur-burning monosodium glutamate wastewater treatment process |
| CN108211740B (en) * | 2018-02-10 | 2024-05-31 | 宁夏洪腾科技开发有限公司 | Silicon carbide smelting tail gas recovery system and tail gas recovery method thereof |
| CN110368816A (en) | 2018-04-13 | 2019-10-25 | 江苏新世纪江南环保股份有限公司 | A kind of method for oxidation and device of ammonia process of desulfurization solution |
| CN110732227B (en) | 2018-07-20 | 2023-02-21 | 江南环保集团股份有限公司 | Method and device for treating acid gas |
| CN109268849A (en) * | 2018-10-27 | 2019-01-25 | 山东默锐环境产业股份有限公司 | A kind of low temperature incinerator and the processing of bromide fire retardant tailing and bromine recyclable device |
| CN109351162B (en) * | 2018-12-06 | 2024-03-12 | 清华大学 | Flue gas treatment equipment of high-temperature heating system |
| CN110052119B (en) * | 2019-03-26 | 2021-12-07 | 昆明理工大学 | Method for absorbing and concentrating hydrogen sulfide in industrial acid gas by organic solvent and utilizing resources |
| CN110508116A (en) * | 2019-09-19 | 2019-11-29 | 中节能工程技术研究院有限公司 | Waste printed circuit board melting gas cleaning recovery system |
| CN111957183A (en) | 2019-12-26 | 2020-11-20 | 江苏新世纪江南环保股份有限公司 | Improved ammonia desulphurization method for controlling aerosol generation in absorption process |
| CN111249869A (en) * | 2020-03-17 | 2020-06-09 | 中国华能集团清洁能源技术研究院有限公司 | Coal chemical industry process waste gas desulfurization device and use method thereof |
| CN116603369A (en) * | 2023-04-28 | 2023-08-18 | 成都益志科技有限责任公司 | Absorbent capable of efficiently absorbing sulfur dioxide |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11179146A (en) * | 1997-12-18 | 1999-07-06 | Chiyoda Corp | Waste gas treatment system |
| CN201988324U (en) * | 2010-11-05 | 2011-09-28 | 合肥宁垣工程技术有限责任公司 | Multi-section combined desulfurizer |
| CN201880478U (en) * | 2010-11-05 | 2011-06-29 | 合肥宁垣工程技术有限责任公司 | Sulphur recycling system for acid gas |
-
2013
- 2013-06-20 CN CN201310245931.3A patent/CN103301732B/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10207220B2 (en) | 2017-03-15 | 2019-02-19 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
| US10016721B1 (en) | 2017-05-25 | 2018-07-10 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desufurization process and apparatus |
| US10092877B1 (en) | 2017-05-25 | 2018-10-09 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10213739B2 (en) | 2017-05-25 | 2019-02-26 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10099170B1 (en) | 2017-06-14 | 2018-10-16 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US10159929B1 (en) | 2017-06-14 | 2018-12-25 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US20190001267A1 (en) | 2017-07-03 | 2019-01-03 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10112145B1 (en) | 2017-09-07 | 2018-10-30 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103301732A (en) | 2013-09-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103301732B (en) | Device and process for recycling and treating hydrogen sulfide-containing chemical acid waste gas | |
| CN102198365B (en) | Processing method of acid gas | |
| CN106430116B (en) | A method of the sulphur-bearing waste solution extracting sulfuric acid generated using coal gas wet oxidation method | |
| CN101934191B (en) | Method for desulfurizing and denitrating smoke simultaneously through ammonia method | |
| CN203342639U (en) | Recovery treatment device for chemical acid waste gas containing hydrogen sulfide | |
| WO2014172860A1 (en) | Method and apparatus for treating acidic tail gas by using ammonia process flue gas | |
| CN205653162U (en) | System for sulphuric acid is prepared to sulphur waste liquid that contains that utilizes coal gas wet oxidation process to produce | |
| CN106310943B (en) | A kind of sodium sulfite desulfurization regeneration and recycling sulfur dioxide device and application | |
| CN104197343B (en) | Oxygen-enriched combustion recycle flue gas catalytic desulfurization system and method | |
| CN106379868A (en) | Method for preparing sulfuric acid by burning sulfur-containing waste liquid | |
| CN106422713A (en) | Method for desulfuration, denitration and dust removal through ultrasonic atomization | |
| CN104560223B (en) | A kind of gas desulfurizer and method thereof | |
| CN102151475B (en) | Two-tower ammonia method desulfurization device and method | |
| CN104524935A (en) | Single-tower type double-circulation sprinkling composite absorption device and method | |
| CN209530493U (en) | A kind of system of Industrial Boiler flue gas desulfurization and denitrification | |
| CN105032173A (en) | Device and process of ammonia-soda-process combined desulfurization and denitrification | |
| CN105692563B (en) | SWSR-7 sulfur recovery technologies and device | |
| CN105771573A (en) | System and method for achieving low-temperature simultaneous desulfurization, denitration and dedusting of flue gas of gas-fired boiler | |
| CN105271132A (en) | SWSR-6 sulfur recovery technology and apparatus thereof | |
| CN106422712A (en) | High-pressure spray desulfurization, denitration and dust removal method | |
| CN101185828B (en) | Waste gas treatment method in glassine production process | |
| CN109647146A (en) | A kind of system and method for Industrial Boiler flue gas desulfurization and denitrification | |
| CN202105585U (en) | Double-oxidation ammonia desulphurization device | |
| CN206229169U (en) | The system for desulfuration and denitration of flue gases of cock oven | |
| CN109701385A (en) | A kind of new catalytic method desulfurizer and technique for coke oven flue gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150121 Termination date: 20180620 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |