CN104326486A - Device for producing ammonium sulfate by using waste sulphur generated during gas desulfuration - Google Patents
Device for producing ammonium sulfate by using waste sulphur generated during gas desulfuration Download PDFInfo
- Publication number
- CN104326486A CN104326486A CN201410604377.8A CN201410604377A CN104326486A CN 104326486 A CN104326486 A CN 104326486A CN 201410604377 A CN201410604377 A CN 201410604377A CN 104326486 A CN104326486 A CN 104326486A
- Authority
- CN
- China
- Prior art keywords
- sulphur
- tower
- heat
- absorption tower
- interchanger
- 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.)
- Granted
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
- Industrial Gases (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a device for producing ammonium sulfate by using waste sulphur generated during gas desulfuration. The device comprises a continuous sulphur melting purifier and a sulphide concentrate clarifying tank which are connected, wherein the sulphide concentrate clarifying tank is connected with a primary oxygenizer through a refined sulphur pump, the primary oxygenizer is connected with a secondary oxygenizer, the secondary oxygenizer is connected with a cold-hot exchanger, the cold-hot exchanger is connected with the top of a first absorption column, the first absorption column is connected with an absorption heat exchanger and also connected with a water tank, the water tank supplies water to the absorption heat exchanger and the first absorption column through a water circulating pump, the primary oxygenizer, the secondary oxygenizer and the heat exchanger are connected with an air outlet of a drying tower, the drying tower is connected with a draught fan, the heat exchanger is connected with a mother solution absorption column, the mother solution absorption column is connected with a mother solution saturator, the top of the mother solution absorption column is connected to the bottom of a tail gas tower, the bottom of the mother solution absorption column is connected with an ammonium sulfate system, and tail gas is discharged by a tail gas chimney. The device provided by the invention can solve the pollution caused by unmarketable waste sulphur and stock piling of waste sulphur, and can change wastes into products, so that wastes can be changed into valuables.
Description
Technical field
The present invention relates to coking chemical technical field, particularly a kind of sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium, is widely used in the coal gas desulfurization field of coke-oven plant and producer gas plant.
Background technology
HPF is the common coal gas desulfurization method of coker.The method take ammonia as alkali source, HPF be catalyzer (quinone, cobalt, iron complexes) by liquid-phase catalytic oxidation, the sulfur-containing impurities such as the hydrogen sulfide in coal gas are converted into elemental sulfur.Elemental sulfur in doctor solution, owing to being reclaimed by pneumatic flotation, also contains the impurity such as a large amount of moisture and coke powder, coal dust, tar, thiocyanate-, thiosulphate and desulfurization catalyst residue in the elemental sulfur of recovery.Traditional technology adopts filter press technique and scorification recovery sulphur wherein usually.Employing filter press technique reclaims, and owing to limitting by filtering equipment filtration efficiency, in the sulphur that filter press technique reclaims, water-content is not less than 20% usually, still containing many water-soluble substanceses, and ammonium thiocyanate, ammonium thiosulfate, ammonium sulfate and desulfurization catalyst etc.; Employing scorification reclaims, and because residence time design is less than normal and the design of equipment side line position is improper, interphase impurity often brings sulphur into, as tar, thiocyanate-and thiosulphate etc.And traditional filter press technique and scorification all adopt interrupter method to operate, separating effect is unstable, and operation site environment is poor, therefore the sulphur obtained by traditional technology is often in paste, and foreign matter content is many, color grey or black, market sale difficulty, production scene is stacked in a large number, seriously polluted.Cause a large amount of waste and the loss of coke-oven plant's element sulphur.
And on the other hand, in the process that coke-oven gas purify at deamination, need again outsourcing sulfuric acid, its principle is in Spray Saturator, add sulfuric acid, and the ammonia in coal gas carries out neutralization reaction, generation ammonium sulfate, and its reaction formula is:
NH
3+2H
2SO
4→2NH
4HSO
4，
NH
4HSO
4+NH
3→(NH
4)
2SO
4
By the ratio control of sulphur and ammonia in saturex, finally generate neutral salt ammonium sulfate, then obtain ammonium sulfate crystallization product by crystallization, often produce 1 ton of ammonium sulfate consumption sulfuric acid and be about 750kg/t.
Obtain sulfur waste for coal gas desulfurization cannot utilize, simultaneously the situation that ammonium sulfate needs to mend sulphur produced by saturex, and the present invention proposes a kind of utilize coal gas desulfurization to produce device that ammonium sulfate is produced in sulfur waste containing tar, secondary salt and saturex coproduction.
Summary of the invention
Object of the present invention is exactly the problems referred to above existed for solving prior art, provides a kind of sulfur waste utilizing coal gas desulfurization to produce to produce the device of ammonium sulfate; Ammonium sulfate is produced in sulfur waste and saturex coproduction that the present invention utilizes coal gas desulfurization to produce containing tar, secondary salt, and the pollution solving the unsalable of sulfur waste and bring due to stacking, realizing refuse derived is product, turns waste into wealth.
The technical scheme of technical solution problem of the present invention is:
A kind of sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium, comprise continuous sulfur melting cleaner, described continuous sulfur melting cleaner comprises the broken bubble section on top, middle de-clear section, the de-slag section of bottom, be connected with supernatant essence sulphur groove bottom described continuous sulfur melting cleaner, supernatant essence sulphur groove is connected with smart sulphur pump, essence sulphur pump is connected with stair oxidation device by pipeline, the stair oxidation device producing high-temperature gas is connected with the waste heat boiler reclaiming high-temperature gas waste heat, waste heat boiler is connected with secondary oxidation device, secondary oxidation device respectively with cold-hot interchanger, heat-heat exchanger, interchanger connects, described cold-hot interchanger is connected with the first top, absorption tower, be connected with cold-hot exchanger base bottom first absorption tower, first top, absorption tower is connected with absorption heat-exchange device, be connected with tank bottom first absorption tower, absorption heat-exchange device water upper with circulation, circulating backwater connects, tank by water circulating pump to absorption heat-exchange device, supply water in first absorption tower, tank is connected with tank, tank is connected with drying tower top by cyclic acid pump, drying tower bottom is connected with tank, tank is connected with aqua storage tank, aqua storage tank also directly can connect user side by water pump, secondary oxidation device, interchanger is connected with drying tower air outlet respectively, stair oxidation device is connected with drying tower air outlet, air from drying tower enters stair oxidation device again after interchanger preheating, drying tower is connected with blower fan, interchanger is connected with bottom mother liquor absorption tower, mother liquor absorption tower is connected with mother liquor saturex, top, mother liquor absorption tower is connected with bottom tail gas tower, be connected with sulphur ammonium system bottom mother liquor absorption tower, tail gas tower respectively with ammonium sulfate system, strong aqua container, ammonia steaming system connects, tail gas tower is also connected with remained ammonia container before ammonia still process, tail gas is discharged by tail gas funnel.
Described secondary oxidation device comprises four sections of catalyzed reaction structures, comprise first stage reaction structure successively from top to bottom, subordinate phase reaction structure, phase III reaction structure, fourth stage reaction structure, first stage reaction structure is connected with heat-heat exchanger, furnace gas after first stage reaction structure catalyst reaction enters heat-heat exchanger through piping, subordinate phase reaction structure is entered after cooling, furnace gas after subordinate phase reaction structure catalyst reaction is through entering phase III reaction structure with after dried freezing air cold shock cooling, after the cooling of cold-hot interchanger, the first absorption tower is entered after reaction, the furnace gas after sulphur trioxide SO3 is absorbed through cold-hot interchanger through the first absorption tower, heat-heat exchanger, utilize the reaction heat of secondary oxidation device to be heated to 420 DEG C and enter fourth stage reaction structure, fourth stage reaction is connected with interchanger, furnace gas after fourth stage reaction structure catalyst reaction, after interchanger cooling, enter mother liquor absorption tower carry out circulating mother liquor absorption.
The water of condensation of described continuous sulfur melting cleaner is connected with coke-oven plant water of condensation house steward, the steam that continuous sulfur melting cleaner produces is connected with coke-oven plant's steam manifold, the desulfurization clear liquid of continuous sulfur melting cleaner is connected with the desulfurization liquid bath of coke-oven plant's desulfurization process, and the sulphur slag of described continuous sulfur melting cleaner is transported to the coal yard coal blending of coke-oven plant.
The steam condensate of described supernatant essence sulphur groove is connected with condensate pipe.
Beneficial effect of the present invention:
1. the present invention utilizes coal gas desulfurization to produce and produces ammonium sulfate containing tar, the sulfur waste of secondary salt and saturex coproduction, solve sulfur waste unsalable and owing to stacking the pollution brought, can make the ammonium sulfate volume increase about 30% of coke-oven plant, realizing refuse derived is product, turns waste into wealth.
2. the present invention adopts continuous sulfur melting cleaner, and compared with traditional coking sulfur melting kettle, production can realize serialization, the remarkable improvement of sulphur color and luster, and purity is increased to 95% by original 70-85%, and molten sulphur purification efficiency significantly improves.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Embodiment
In order to understand the present invention better, explain embodiments of the present invention in detail below in conjunction with accompanying drawing.
Embodiment 1:
As shown in Figure 1, by sulfur-bearing 15.5%, moisture 80.9%, other impurity 3.6% (comprising coke powder, coal dust, tar, ammonium thiocyanate, ammonium thiosulfate, ammonium sulfate, catalyst residue), after continuous sulfur melting purification utensil, the purity obtaining sulphur is 99.6%.
The sulphur of sulfur-bearing 99.5% (is comprised first grade absorption tower) after secondary oxidation, and the composition (volume %) obtaining gas is SO
2: 0.059%, SO
3: 0.308%, O
2: 12.023%, N
2: 87.61%.
SO is consisted of by above-mentioned
2: 0.059%, SO
3: 0.308%, O
2: 12.023%, N
2: the gas of 87.61% absorbs (mother liquor proportion 1.26g/cm with sulphur ammonium circulating mother liquor
3, crystallization ratio is less than 10%, mother liquor acidity 3.5-4.5%, liquid-gas ratio (V/V) 1:10; And then with strong aqua (10%, wt) absorb after, gas consist of SO
2concentration ﹤ 400mg/Nm
3, sulfuric acid mist ﹤ 30mg/Nm
3, particulate matter ﹤ 50mg/Nm
3.
A kind of sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium, comprise continuous sulfur melting cleaner 1, described continuous sulfur melting cleaner 1 comprises the broken bubble section on top, middle de-clear (liquid) section, the de-slag section of bottom, be connected with supernatant essence sulphur groove 2 bottom described continuous sulfur melting cleaner, supernatant essence sulphur groove 2 is connected with smart sulphur pump 11, essence sulphur pump 11 is connected with stair oxidation device 3 by pipeline, the stair oxidation device 3 producing high-temperature gas is connected with the waste heat boiler 12 reclaiming high-temperature gas waste heat, waste heat boiler 12 is connected with the secondary oxidation device 4 of low temperature absorption, secondary oxidation device 4 respectively with cold-hot interchanger 13, heat-heat exchanger 14, interchanger 15 connects, described cold-hot interchanger 13 is connected with the first top, absorption tower 5, be connected with bottom cold-hot interchanger 13 bottom first absorption tower 5, first top, absorption tower 5 is connected with absorption heat-exchange device 16, be connected with tank 17 bottom first absorption tower 5, absorption heat-exchange device 16 water upper with circulation, circulating backwater connects, tank 17 passes through water circulating pump 22 to absorption heat-exchange device 16, supply water in first absorption tower 5, tank 17 is connected with tank 18, tank 18 is connected with drying tower 6 top by cyclic acid pump 23, drying tower 6 bottom is connected with tank 17, tank 18 is connected with aqua storage tank 19, aqua storage tank 19 also directly can connect user side by water pump 21, secondary oxidation device 4, interchanger 15 is connected with drying tower 6 air outlet respectively, stair oxidation device 3 is connected with drying tower 6 air outlet, air from drying tower 6 enters stair oxidation device 3 again after interchanger 15 preheating, drying tower 6 is connected with blower fan 9, interchanger 15 is connected with bottom mother liquor absorption tower 7, mother liquor absorption tower 7 is connected with mother liquor saturex, top, mother liquor absorption tower 7 is connected with bottom tail gas tower 8, be connected with sulphur ammonium system bottom mother liquor absorption tower 7, Recycling Mother Solution is connected with top, mother liquor absorption tower by pipeline bottom mother liquor absorption tower simultaneously, tail gas tower 8 respectively with ammonium sulfate system, strong aqua container, ammonia steaming system connects, tail gas tower is also connected with remained ammonia container before ammonia still process simultaneously, tail gas is discharged by tail gas funnel 81.
Described secondary oxidation device 4 comprises four sections of catalyzed reaction structures, comprise first stage reaction structure 41 successively from top to bottom, subordinate phase reaction structure 42, phase III reaction structure 43, fourth stage reaction structure 44, first stage reaction structure 41 is connected with heat-heat exchanger 14, furnace gas after first stage reaction structure 41 catalyst reaction enters heat-heat exchanger 14 through piping, subordinate phase reaction structure 42 is entered after cooling, furnace gas after subordinate phase reaction structure 42 catalyst reaction is through entering phase III reaction structure 43 with after dried freezing air cold shock cooling, after cold-hot interchanger 13 is lowered the temperature, the first absorption tower 5 is entered after reaction, sulphur trioxide (SO is absorbed through the first absorption tower 5
3) after furnace gas through cold-hot interchanger 13, heat-heat exchanger 14, utilize the reaction heat of secondary oxidation device to be heated to 420 DEG C to enter fourth stage reaction structure, fourth stage reaction 44 is connected with interchanger 15, react the reacted furnace gas of 44 structure catalyst through fourth stage, after interchanger 15 is lowered the temperature, enter mother liquor absorption tower 7 carry out circulating mother liquor absorption.
Principle of work of the present invention is:
1) purification of sulfur waste
The sulfur waste (or claiming sulphur foam) that gas desulfurization processes produces, due to containing impurity such as a large amount of moisture and coke powder, coal dust, tar, thiocyanate-, thiosulphate and desulfurization catalyst residues, first needs purification.Due to traditional filter press technique and scorification recovering effect not good, this patent adopts continuous sulfur melting cleaner to carry out the purification of sulfur waste.Continuous sulfur melting cleaner is made up of three parts, and first part is broken bubble section, and the sulphur foam carrying out bin cure foam pump is at foam section by steam or heat-conducting oil heating to 70 DEG C-80 DEG C, and make sulphur bubble collapse, sulfur granules progressively sinks.The liquid that broken bubble section flows out enters upright de-clear (liquid) section, at this pars infrasegmentalis, sulfur granules is heated to 120 DEG C-150 DEG C, sulphur is made to be fused into liquid, the clear liquid brought into of sulphur foam due to density less, float up to the de-clear continuous extraction in (liquid) section top, the clear liquid of extraction returns coal gas desulfurization workshop section and supplements doctor solution use.The air formed after sulphur lather collapse since then section top is released, and releases speed and determines depending on ullage gaseous pressure, then open vent valve usually above 3-5kg/cm2; De-clear (liquid) section forms the temperature distribution progressively reduced from bottom to top due to the heating of bottom coil pipe, and the sulphur slag of bottom liquefaction flows into de-slag section, and by sulphur slag less for the density that contains from de-slag section portion's extraction, the extraction of sulphur slag returns coal yard coal blending and uses.The sulfur purity flowed out continuously bottom sulphur section can reach 99%-99.5%, to enter before stair oxidation device with the melting of agitator continuously stirring as Molten sulphur overflow enters subsider, molten sulfur overflow after supernatant enters smart sulphur groove, the equipment of the as a whole structure of described supernatant essence sulphur groove, divide supernatant and rectifying two portions, wherein the steam condensate of supernatant essence sulphur groove returns condensate pipe.Molten sulfur is pumped into oxidizer by smart sulphur and is oxidized.The water of condensation of continuous sulfur melting cleaner returns coke-oven plant water of condensation house steward in addition, generation steam is incorporated to coke-oven plant's steam manifold, and desulfurization clear liquid returns the desulfurization liquid bath of coke-oven plant's desulfurization process, the coal yard coal blending of Liu Zhaqu coke-oven plant.
(2) oxidation of rectifying.
Smart sulphur (liquid) through purification is sent in stair oxidation stove through mechanical nozzle, produces SO with atmospheric oxidation
2gas; Stair oxidation required air, by air-blaster, is sent in stair oxidation device after sending into drying tower drying.Go out the SO after stair oxidation device
2furnace gas passes into artificial atmosphere SO through the cooling of waste heat boiler recovery waste heat, then Sustainable Control
2concentration enters secondary oxidation device, by SO wherein to 9-9.5%, temperature about 420 DEG C
2continue to be oxidized to SO
3.Secondary oxidation device adopts four sections of catalyzed oxidations.Furnace gas after first paragraph catalyst reaction enters heat-heat exchanger, enters second segment catalyzer after cooling.Furnace gas after second segment catalyst reaction is through entering the 3rd section of catalyzer with after dried freezing air cold shock cooling.Through cold-hot interchanger after reaction, after cooling, enter the first absorption tower.Absorb SO wherein
3after furnace gas through cold-hot interchanger, heat-heat exchanger and utilize the reaction heat of secondary oxidation device to be heated to 420 DEG C to enter convertor and carry out the 4th section of catalyzer, furnace gas after the 4th section of catalyst reaction, carries out circulating mother liquor absorption to enter mother liquor absorption tower after air heat exchanger cooling.
(3) mother liquor absorbs and tail gas absorption
Because containing (NH in the circulating mother liquor of sulphur ammonium saturex
4)
2sO
4, following reaction can be there is,
(NH
4)
2SO
4+SO
3+H
2O→2NH
4HSO
4(1)
According to formula (1), the present invention adopts the circulating mother liquor of sulphur ammonium saturex, absorbs from the SO in tail gas after the cooling of secondary oxidation device in mother liquor absorption tower
3.And then through tail gas absorber absorption SO wherein
2.Tail gas absorber is divided into two parts, and top is divided into remained ammonia absorber portion, and bottom is divided into strong aqua absorber portion.Enter mother liquor tail gas from absorption tower and the cyclic absorption ammoniacal liquor counter current contact of tail gas absorber bottom, the SO in gas
2be recycled liquid and absorb generation ammonium bisulfite, shown in (2).
NH
3+SO
2+H
2O→NH
4HSO
3(2)
Under the condition filling into air, in tower, be oxidized to monoammonium sulfate, shown in (3) simultaneously.
2NH
4HSO
3+O
2→2NH
4HSO
4(3)
Monoammonium sulfate reacts with 10% ammoniacal liquor filling into system and generates ammonium sulfate, shown in (4).
NH
4HSO
4+NH
3→(NH
4)
2SO
4(4)
According to the amount filling into 10% ammoniacal liquor, in liquid to be recycled, ammonium sulfate reaches finite concentration (about 10%), this circulation fluid part is expelled to the sulphur crystalline ammonium device of sulphur ammonium saturex system, obtains ammonium sulfate by crystallization.
Gas after tail gas absorber hypomere absorbs enters tail gas absorber epimere, absorbs acid mist in captured gas and volatilization ammonia with remained ammonia, and the liquid after absorption removes ammonia still process from extraction in the middle part of tail gas absorber.
SO after tail gas absorber in gas
2content is ﹤ 400mg/Nm
3, lower than discharging standards GB2132-2010, by chimney emptying.
(4) dryer section of air
Oxidising process required air enters drying tower after gas blower pressurization, through 98% sulfuric acid absorption moisture, makes moisturely to be down to≤0.1g/Nm
3, and enter after foam removal after air preheater is preheated to 300 DEG C and enter stair oxidation device.In drying tower, spray acid carries out sour circulation groove after going out tower, adds water and regulates its concentration, sends into drying tower acid cooler to cool laggard drying tower spray with cyclic acid pump.
First absorption tower also adopts in 98% sulfuric acid absorption secondary oxidation device, three sections of catalysis extraction gas and generates sulfuric acid, continue to be fed in saturex and spray, and the ammonia in coal gas carries out neutralization reaction, generates sulphur ammonium.
By reference to the accompanying drawings the embodiment of invention is described although above-mentioned; but not limiting the scope of the invention; on the basis of technical scheme of the present invention, those skilled in the art do not need to pay various amendment or distortion that creative work can make still within protection scope of the present invention.
Claims (4)
1. the device of the sulfur waste production sulphur ammonium utilizing coal gas desulfurization to produce, it is characterized in that, comprise continuous sulfur melting cleaner, described continuous sulfur melting cleaner comprises the broken bubble section on top, middle de-clear section, the de-slag section of bottom, be connected with supernatant essence sulphur groove bottom described continuous sulfur melting cleaner, supernatant essence sulphur groove is connected with smart sulphur pump, essence sulphur pump is connected with stair oxidation device by pipeline, the stair oxidation device producing high-temperature gas is connected with the waste heat boiler reclaiming high-temperature gas waste heat, waste heat boiler is connected with secondary oxidation device, secondary oxidation device respectively with cold-hot interchanger, heat-heat exchanger, interchanger connects, described cold-hot interchanger is connected with the first top, absorption tower, be connected with cold-hot exchanger base bottom first absorption tower, first top, absorption tower is connected with absorption heat-exchange device, be connected with tank bottom first absorption tower, absorption heat-exchange device water upper with circulation, circulating backwater connects, tank by water circulating pump to absorption heat-exchange device, supply water in first absorption tower, tank is connected with tank, tank is connected with drying tower top by cyclic acid pump, drying tower bottom is connected with tank, tank is connected with aqua storage tank, aqua storage tank also directly can connect user side by water pump, secondary oxidation device, interchanger is connected with drying tower air outlet respectively, stair oxidation device is connected with drying tower air outlet, air from drying tower enters stair oxidation device again after interchanger preheating, drying tower is connected with blower fan, interchanger is connected with bottom mother liquor absorption tower, mother liquor absorption tower is connected with mother liquor saturex, top, mother liquor absorption tower is connected with bottom tail gas tower, be connected with sulphur ammonium system bottom mother liquor absorption tower, tail gas tower respectively with ammonium sulfate system, strong aqua container, ammonia steaming system connects, tail gas tower is also connected with remained ammonia container before ammonia still process, tail gas is discharged by tail gas funnel.
2. the sulfur waste utilizing coal gas desulfurization to produce as claimed in claim 1 produces the device of sulphur ammonium, it is characterized in that, described secondary oxidation device comprises four sections of catalyzed reaction structures, comprise first stage reaction structure successively from top to bottom, subordinate phase reaction structure, phase III reaction structure, fourth stage reaction structure, first stage reaction structure is connected with heat-heat exchanger, furnace gas after first stage reaction structure catalyst reaction enters heat-heat exchanger through piping, subordinate phase reaction structure is entered after cooling, furnace gas after subordinate phase reaction structure catalyst reaction is through entering phase III reaction structure with after dried freezing air cold shock cooling, after the cooling of cold-hot interchanger, the first absorption tower is entered after reaction, sulphur trioxide SO is absorbed through the first absorption tower
3after furnace gas through cold-hot interchanger, heat-heat exchanger, utilize the reaction heat of secondary oxidation device to be heated to 420 DEG C and enter fourth stage reaction structure, fourth stage reaction is connected with interchanger, furnace gas after fourth stage reaction structure catalyst reaction, enters mother liquor absorption tower and carries out circulating mother liquor absorption after interchanger cooling.
3. the sulfur waste utilizing coal gas desulfurization to produce as claimed in claim 1 produces the device of sulphur ammonium, it is characterized in that, the water of condensation of described continuous sulfur melting cleaner is connected with coke-oven plant water of condensation house steward, the steam that continuous sulfur melting cleaner produces is connected with coke-oven plant's steam manifold, the desulfurization clear liquid of continuous sulfur melting cleaner is connected with the desulfurization liquid bath of coke-oven plant's desulfurization process, and the sulphur slag of described continuous sulfur melting cleaner is transported to the coal yard coal blending of coke-oven plant.
4. the sulfur waste utilizing coal gas desulfurization to produce as claimed in claim 1 produces the device of sulphur ammonium, it is characterized in that, the steam condensate of described supernatant essence sulphur groove is connected with condensate pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410604377.8A CN104326486B (en) | 2014-10-30 | 2014-10-30 | The sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410604377.8A CN104326486B (en) | 2014-10-30 | 2014-10-30 | The sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104326486A true CN104326486A (en) | 2015-02-04 |
| CN104326486B CN104326486B (en) | 2016-04-13 |
Family
ID=52401315
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410604377.8A Active CN104326486B (en) | 2014-10-30 | 2014-10-30 | The sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104326486B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104773885A (en) * | 2015-03-26 | 2015-07-15 | 潍坊特钢集团有限公司 | Comprehensive treatment method of coking desulfurization waste liquid |
| CN111232934A (en) * | 2020-03-19 | 2020-06-05 | 四川华茂聚源建筑工程设计有限公司 | Device for utilizing desulfurization waste liquid and operation method thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102951657A (en) * | 2012-12-10 | 2013-03-06 | 张卫东 | Process and equipment for producing ammonium sulfate by taking sulfur pulp and ammonia water as raw materials |
| CN103060019A (en) * | 2013-02-01 | 2013-04-24 | 济钢集团有限公司 | Self-circulation desulfurization device and desulfurization method |
| CN104229755A (en) * | 2013-06-24 | 2014-12-24 | 王荷琴 | Method for preparing sulfuric acid from sulfur |
| CN204237569U (en) * | 2014-10-30 | 2015-04-01 | 济南冶金化工设备有限公司 | The sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium |
-
2014
- 2014-10-30 CN CN201410604377.8A patent/CN104326486B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102951657A (en) * | 2012-12-10 | 2013-03-06 | 张卫东 | Process and equipment for producing ammonium sulfate by taking sulfur pulp and ammonia water as raw materials |
| CN103060019A (en) * | 2013-02-01 | 2013-04-24 | 济钢集团有限公司 | Self-circulation desulfurization device and desulfurization method |
| CN104229755A (en) * | 2013-06-24 | 2014-12-24 | 王荷琴 | Method for preparing sulfuric acid from sulfur |
| CN204237569U (en) * | 2014-10-30 | 2015-04-01 | 济南冶金化工设备有限公司 | The sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104773885A (en) * | 2015-03-26 | 2015-07-15 | 潍坊特钢集团有限公司 | Comprehensive treatment method of coking desulfurization waste liquid |
| CN111232934A (en) * | 2020-03-19 | 2020-06-05 | 四川华茂聚源建筑工程设计有限公司 | Device for utilizing desulfurization waste liquid and operation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104326486B (en) | 2016-04-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103303872B (en) | System device and method for recycling sulfur dioxide from fume to prepare sulfur | |
| CN104528659B (en) | Sulfur recycling process for circularly treating low-concentration acidy gas by utilizing liquid sulfur | |
| CN110040691B (en) | Device and method for preparing and producing high-purity sulfur dioxide by using acid gas | |
| CN102381687A (en) | Method for preparing acid by using sulfur containing waste material and wet method desulphurization process containing method thereof | |
| CN206553478U (en) | Coal oven dithio-gas purifier | |
| CN211521596U (en) | System for preparing analytically pure sulfuric acid from smelting flue gas | |
| CN101723334A (en) | Raw material pretreatment process for preparing sulfuric acid by using low-quality sulfur and sulphur-bearing waste solution | |
| CN105600990A (en) | Method for recycling coke oven gas desulfurization and decyanation waste liquid to reclaim sulfur, ammonium sulfate and catalysts | |
| CN104548902A (en) | Acetylene gas purification device and process thereof | |
| EP3679164A1 (en) | Plant and method for the thermal treatment of solids | |
| CN105217580A (en) | A kind of electrolytic manganese residues high temperature desulfurizing enriched flue gas prepares the method for sulfuric acid | |
| CN107823906A (en) | A kind of raw gas conversion process condensate liquid stripping processing system and method | |
| CN104986740A (en) | Claus tail gas treatment system and treatment method | |
| CN101624197B (en) | Technology for calcining and recycling magnesium desulfurizing byproduct containing magnesium sulfite | |
| CN104326486B (en) | The sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium | |
| CN204237569U (en) | The sulfur waste utilizing coal gas desulfurization to produce produces the device of sulphur ammonium | |
| CN111115587A (en) | Method and system for preparing analytically pure sulfuric acid from smelting flue gas | |
| CN106672904A (en) | Method for comprehensively treating sulfur-containing flue gas and solid waste abraum salt | |
| CN105727714B (en) | A kind of process and device for producing NaHS | |
| CN105731497B (en) | A kind of utilization sour gas produces the method and device of sodium acid carbonate | |
| CN105642090B (en) | A kind of Acidic Gas Treating method and device | |
| CN202569933U (en) | Special device for processing method of preparing sodium sulphide by hydrogen sulfide acid gas | |
| CN105731501B (en) | A kind of utilization sour gas produces the method and device of solid sodium bicarbonate | |
| CN107376618A (en) | A kind of hydrogenation purification method of Sulfur Recovery Unit tail gas | |
| CN105727715B (en) | A kind of Acidic Gas Treating technique and system |
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 | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A device for producing ammonium sulfate from waste sulfur generated by gas desulfurization Effective date of registration: 20230317 Granted publication date: 20160413 Pledgee: Postal Savings Bank of China Limited Jinan Changqing District sub branch Pledgor: JINAN METALLURGY CHEMICAL EQUIPMENT CO.,LTD. Registration number: Y2023980035136 |