CN203033778U - Device for producing ammonium sulfate by using sulfate pulp and ammonia water as raw materials - Google Patents
Device for producing ammonium sulfate by using sulfate pulp and ammonia water as raw materials Download PDFInfo
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- CN203033778U CN203033778U CN201220680333XU CN201220680333U CN203033778U CN 203033778 U CN203033778 U CN 203033778U CN 201220680333X U CN201220680333X U CN 201220680333XU CN 201220680333 U CN201220680333 U CN 201220680333U CN 203033778 U CN203033778 U CN 203033778U
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- CN
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- Prior art keywords
- ammonium sulfate
- outlet
- thionizer
- mother liquor
- liquor
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- 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
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Abstract
The utility model relates to a device for producing ammonium sulfate by using sulfate pulp and ammonia water as raw materials. The device comprises a combustion furnace, a waste heat boiler, an evaporation crystallizer, a mother liquor heating device, a cooling device, a desulfurizing tower and a ammonium sulfate mother liquor tank. A combustion furnace outlet is connected with the waste heat boiler through a smoke channel, a waste heat boiler outlet is connected with the evaporation crystallizer through the smoke channel, the evaporation crystallizer is connected with the mother liquor heating device through a circulating pump, a mother liquor heating device outlet is connected with an upper sprayer in the evaporation crystallizer through a pipeline, an outlet of the top of the evaporation crystallizer is connected with the cooling device through a fan, and a cooling device outlet is connected with the lower portion of the desulfurizing tower. The bottom of the evaporation crystallizer is provided with an outlet of the ammonium sulfate mother liquor containing crystal, and the outlet of the ammonium sulfate mother liquor containing crystal is connected with an ammonium sulfate crystallizing device. The device produces ammonium sulfate products and solves the problem that low-quality sulfate pulp is further separated and processed and ammonia water can not be sold. Simultaneously, the sulfate pulp is used for replacing sulfuric acid required to be purchased during production of the ammonium sulfate, and resources are used comprehensively.
Description
Technical field
The utility model relates to technical field of coal chemical industry, particularly desulfurization and deamination technology and device in the coke oven gas purification engineering.
Background technology
In process of coking, contain 4～8g/m in the coke-oven gas approximately
3H
2S and 0.15～2g/m
3HCN.If do not remove, contain H
2When the coal gas of S and HCN acts as a fuel burning, can generate a large amount of SO
2And NOx, thereby cause serious topsoil.In the coke oven gas desulfurization Technology, extensively adopt Wet-type oxidation sweetening technology at present, representing technology is FRC technology and PDS technology.The doctor solution of this technology is alkali source with the ammonia in the coal gas.H in the coal gas
2Absorption, the oxidation regeneration of S by doctor solution is converted into the sulphur slurry of sulphur, ammonium thiosulfate and ammonium thiocyanate, and the advantage of this technology is the desulfuration efficiency height, need not exogenously added alkali, and process cost is low.Shortcoming is foreign matter content height in the sulphur slurry, and the sulphur slurry can't be sold as product, needs further to separate processing.And this complete processing complexity, energy consumption are big and investment is high, and products obtained therefrom does not have economic benefit, and form secondary pollution.
Recovering ammonia technique extensively adopts absorption process to remove ammonia in the coal gas in the coke-oven gas, adopts sulfuric acid absorption---and the characteristics that crystallization process is produced thiamine process are that technical process is simple, but the processing medium seriously corroded, maintenance of equipment expense height also needs outsourcing sulfuric acid simultaneously; Employing phosphoric acid absorbs---and desorption method is produced liquefied ammonia or the ammoniacal liquor process characteristic is that technical process is simple, and working cost is low.Shortcoming is to be subjected to restrictions such as user's condition, storage and transportation, and there are certain difficulty in liquefied ammonia or ammoniacal liquor as production marketing.
The utility model content
It is the equipment of raw material production sulphur ammonium with sulphur slurry and ammoniacal liquor that the purpose of this utility model provides a kind of, by this device fabrication ammonium sulfate products, solve low-quality sulphur slurry and further separated the problem of processing and the problem that ammoniacal liquor can't be sold, utilize the sulphur slurry to substitute the sulfuric acid of required outsourcing when producing the sulphur ammonium simultaneously, resource obtains comprehensive utilization.
For achieving the above object, the utility model is achieved through the following technical solutions:
Be the equipment of raw material production sulphur ammonium with sulphur slurry and ammoniacal liquor, comprise roasting kiln, waste heat boiler, evaporative crystallizer, mother liquor well heater, water cooler, thionizer, ammonium sulfate liquor groove; The roasting kiln outlet is connected by exhaust gases passes with waste heat boiler, the waste heat boiler outlet links to each other with evaporative crystallizer by exhaust gases passes, evaporative crystallizer links to each other with the mother liquor well heater by recycle pump, the mother liquor heater outlet links to each other with evaporative crystallizer internal upper part shower nozzle by pipeline, the evaporative crystallizer top exit is connected with water cooler by blower fan, and cooler outlet is connected with the thionizer bottom; Thionizer middle part and top doctor solution pipe are provided with ammonia inlet, and the thionizer bottom communicates with the ammonium sulfate liquor groove by overflow ducts, and the ammonium sulfate liquor groove is connected with evaporative crystallizer by the connecting tube of ammonium sulfate liquor pump; The evaporative crystallizer bottom is provided with the ammonium sulfate liquor outlet that contains crystallization, is connected with sulphur crystalline ammonium device.
Described evaporative crystallizer peripheral hardware mother liquor well heater, the bottom is provided with recycle pump, send evaporative crystallizer top to spray after by recycle pump ammonium sulfate liquor being delivered to heater heats; The mother liquor well heater heats circulating mother liquor, for the ammonium sulfate liquor evaporation provides auxiliary thermal source, keeps ammonium sulfate liquor water balance in the evaporative crystallizer.
Described thionizer is two sections, and hypomere is empty spray section, and epimere is packing section, and thionizer top is provided with pounces on the mist layer.
Be the technology of raw material production sulphur ammonium with sulphur slurry and ammoniacal liquor, be 15 ~ 20% to be raw material with ammonia concn, ammonium sulfate liquor in the evaporative crystallizer is through cooled flue gas and the heat supply of mother liquor well heater, moisture evaporation makes that the sulphur ammonium concentration reaches 30 ~ 42% in the ammonium sulfate liquor, and the ammonium sulfate liquor of evaporative crystallizer bottom is delivered to sulphur crystalline ammonium device and extracted crystallization through vacuum-evaporation; Be raw material with the anhydrous ammonia that contains ammonia 99.8%, ammonium sulfate liquor in the evaporative crystallizer is through cooled flue gas and the heat supply of mother liquor well heater, make moisture evaporation formation supersaturated solution in the ammonium sulfate liquor, at the bottom of the method for steaming crystallizer, produce crystallization, crystallization apparatus is delivered in crystallization separated.
Compared with prior art, the beneficial effects of the utility model are:
The ammoniacal liquor that the sulphur that this technology produces with coke-oven gas Wet-type oxidation sweetening (ammonia process) technology is starched and coke-oven gas recovery ammonia produces is raw material, produce ammonium sulfate products by producing and manufacturing technique of the present utility model, solve low-quality sulphur slurry and further separated the problem of processing and the problem that ammoniacal liquor can't be sold, utilize the sulphur slurry to substitute the sulfuric acid of required outsourcing when producing the sulphur ammonium simultaneously, resource obtains comprehensive utilization.
Description of drawings
Fig. 1 is structure iron of the present utility model.
Among the figure: 1-roasting kiln 2-waste heat boiler 3-evaporative crystallizer 4-blower fan 5-recycle pump 6-crystallization pump 7-water cooler 8-thionizer 9-hypomere recycle pump 10-epimere recycle pump 11-ammonium sulfate liquor groove 12-ammonium sulfate liquor pump
13-mother liquor well heater
Embodiment
Below in conjunction with accompanying drawing and example equipment of the present utility model and technology are described in further detail.
The sulphur slurry that coke-oven gas Wet-type oxidation sweetening (ammonia process) technology produces sulphur slurry water content after evaporation concentration reaches weight percent 35 ~ 60%.The sulphur slurry is through being pumped to roasting kiln 1, and the sulphur slurry sprays into roasting kiln through atomizing nozzle, and coal gas and air are sent into mixed firing in the roasting kiln 1 after the blower fan pressurization, and coefficient of excess air is controlled in 1.2 ~ 1.3 scopes.Temperature in the roasting kiln reaches 1000 ~ 1200 ゜ C, and sulphur is converted into SO in the sulphur slurry
2High-temperature flue gas is through waste heat boiler 2 heat exchange, high-temperature flue-gas is delivered to evaporative crystallizer 3 after being down to 350 ~ 500 ゜ C, in order to reduce the service temperature of evaporative crystallizer, flue gas mixes air and reduces flue-gas temperature to 150 ~ 250 ゜ C before entering evaporative crystallizer, mix air capacity control in 0.6 ~ 1.5 times scope of exhaust gas volumn.Flue gas is entered by the evaporative crystallizer middle part, by ammonium sulfate liquor pump 12 ammonium sulfate liquor of ammonium sulfate liquor groove 11 is delivered to evaporative crystallizer 3 bottoms, and ammonium sulfate liquor sulfur-bearing ammonium concentration is 30 ~ 42%.Ammonium sulfate liquor is delivered to mother liquor well heater 13 through recycle pump 5, enters the spray cooling of evaporative crystallizer top after the heating, and the moisture evaporation in the ammonium sulfate liquor makes flue gas cooling and saturated.The ammonium sulfate liquor moisture evaporation increases the sulphur ammonium concentration simultaneously, and ammonium sulfate liquor is delivered to sulphur crystalline ammonium device through crystallization pump 6 and extracted crystallization through vacuum-evaporation.The saturated flue gas of evaporative crystallizer outlet enters water cooler 7 after blower fan 4 pressurizations, flue gas enters thionizer 8 after water cooler is cooled to 45 ~ 55 ℃; The phlegma that the flue gas cooling produces effluxes or part is sent thionizer.Enter flue gas and the doctor solution counter current contact of thionizer, thionizer is provided with the two-stage desulfurization section, and hypomere is empty spray section, and epimere is packing section.Each section is respectively equipped with the doctor solution recycle pump, as shown in fig. 1 hypomere recycle pump 9 and epimere recycle pump 10.Doctor solution is delivered to the empty spray section sprinkling of thionizer 8 middle parts through hypomere recycle pump 9 at the bottom of the tower, and doctor solution is delivered to the packing section sprinkling of thionizer top through epimere recycle pump 10 at the bottom of the tower.SO in the flue gas
2SO behind the two-stage desulfurization liquid washing desulphurization of thionizer
2Concentration is lower than 100mg/M
3Flue gas enters atmosphere by the thionizer top after pouncing on the mist layer by cat head.Ammoniacal liquor is delivered in the thionizer circulating-pump outlet doctor solution, and the doctor solution pH value control in the thionizer is 6.0 ~ 6.5, and the thionizer service temperature is controlled at 50 ~ 70 ゜ C.Doctor solution by the thionizer overflow to ammonium sulfate liquor groove 11, (the NH in the doctor solution
4)
2SO
3Be oxidized to (NH during flue gas adverse current contacts
4)
2SO
4, the bubbling air again in ammonium sulfate liquor groove 11 bottoms makes a small amount of (NH in the doctor solution that enters ammonium sulfate liquor groove 11
4)
2SO
3Oxidation transfers (NH to
4)
2SO
4, the ammonium sulfate liquor of ammonium sulfate liquor groove is delivered to evaporative crystallizer 3 through ammonium sulfate liquor pump 12.Doctor solution is through the air reoxidation in the described ammonium sulfate liquor groove, and ammonium sulfate liquor sulphur ammonium concentration reaches 30 ~ 42%.
In this technology, the chemical equation that the sulphur slurry burns in roasting kiln is as follows:
S+O
2=SO
2
NH
4SCN+3O
2=N
2+CO
2+SO
2+2H
2O
2(NH
4)
2S
2O
3+5O
2=2N
2+4SO
2+8H
2O
2H
2+O
2=2H
2O
CH
4+2O
2=CO
2+2H
2O
2CO+O
2=2CO
2
The main chemical reactions of sweetening process is:
NH
3+H
2O+SO
2=NH
4HSO
3
2NH
3+H
2O+SO
2=(NH
4)
2SO
3
(NH
4)
2SO
3+SO
2+H
2O=2NH
4HSO
3
Do following craft embodiment with above-mentioned Processes and apparatus:
Embodiment 1:
Contain 25% sulphur, 20% ammonium thiocyanate, 20% ammonium thiosulfate from the sulphur slurry that the coal gas desulfurization device is sent here, all the other are water.The ammoniacal liquor of sending here from ammonia recovery unit contains ammonia 20%.Coke-oven gas and coefficient of excess are sent into the roasting kiln internal combustion at 1.3 air through the blower fan pressurization, and the sulphur slurry is delivered to atomizing nozzle through the pump pressurization and sprayed into the roasting kiln internal combustion.Flue-gas temperature reaches 1200 ゜ C in the roasting kiln, and flue gas reaches 400 ゜ C after the waste heat boiler heat exchange, and flue gas is through the air blending, and air blending amount is 1.2 times of exhaust gas volumn.The circulating mother liquor spray cooling of flue gas in evaporative crystallizer, the mother liquor well heater increases the evaporation of mother liquor moisture to the circulating mother liquor heat supply, and flue gas is delivered to water cooler after the blower fan pressurization, enter water cooler and be cooled to 58 ゜ C and deliver to thionizer again, flue gas removes SO with the doctor solution counter current contact in thionizer
2, ammoniacal liquor is delivered in the doctor solution of thionizer circulating-pump outlet, removes SO
2Flue gas drained in the atmosphere by the desulfurization cat head, control doctor solution pH value is 6.0.Moisture evaporation concentrates ammonium sulfate liquor in evaporative crystallizer, and ammonium sulfate liquor extracts crystallization through being pumped to sulphur crystalline ammonium device through vacuum-evaporation, and ammonium sulfate liquor returns thionizer.
Embodiment 2:
From the coal gas desulfurization device send here concentrate after the sulphur slurry, contain 10% sulphur, 19% ammonium thiocyanate, 19% ammonium thiosulfate in the sulphur slurry, moisture 48% and other salt impurity.The ammoniacal liquor of sending here from ammonia recovery unit contains ammonia 18%.Coke-oven gas and coefficient of excess are sent into the roasting kiln internal combustion at 1.3 air through the blower fan pressurization, and the sulphur slurry is delivered to atomizing nozzle through the pump pressurization and sprayed into the roasting kiln internal combustion.Flue-gas temperature reaches 1200 ゜ C in the roasting kiln, and flue gas reaches 500 ゜ C after the waste heat boiler heat exchange, and flue gas is through the air blending, and air blending amount is 1.4 times of exhaust gas volumn.The circulating mother liquor spray cooling of flue gas in evaporative crystallizer, the mother liquor well heater is to the circulating mother liquor heat supply, increase the evaporation of mother liquor moisture, flue gas is delivered to water cooler after the blower fan pressurization, deliver to thionizer after being cooled to 60 ゜ C, flue gas in thionizer with the doctor solution counter current contact, ammoniacal liquor is delivered in the doctor solution of thionizer circulating-pump outlet, removes SO
2Flue gas drained in the atmosphere by the desulfurization cat head, control doctor solution pH value is 6.5.Moisture evaporation concentrates ammonium sulfate liquor in evaporative crystallizer, and ammonium sulfate liquor extracts crystallization through being pumped to sulphur crystalline ammonium device through vacuum-evaporation, and ammonium sulfate liquor returns thionizer.
Embodiment 3:
Connect the road from the coal gas desulfurization device send here concentrate after the sulphur slurry, contain 20% sulphur, 19% ammonium thiocyanate, 19% ammonium thiosulfate in the sulphur slurry, moisture 38% and other salt impurity.The anhydrous ammonia of sending here from ammonia recovery unit contains ammonia 99.7%.Coke-oven gas and coefficient of excess are sent into the roasting kiln internal combustion at 1.25 air through the blower fan pressurization, and the sulphur slurry is delivered to atomizing nozzle through the pump pressurization and sprayed into the roasting kiln internal combustion.Flue-gas temperature reaches 1100 ゜ C in the roasting kiln, and flue gas reaches 350 ゜ C after the waste heat boiler heat exchange, flue gas and air blending, and air blending amount is 0.8 times of dry flue gas amount.The mother liquor spray cooling of flue gas in evaporative crystallizer, the mother liquor well heater is to the circulating mother liquor heat supply, increase the evaporation of mother liquor moisture, flue gas is delivered to water cooler after blower fan pressurization, deliver to thionizer after being cooled to 55 ゜ C, and epimere and stage casing spray delivered to doctor solution respectively by recycle pump at the bottom of the tower, partial desulfurization liquid is delivered to the anhydrous ammonia tempering tank, anhydrous ammonia mixes with doctor solution by in the doctor solution that is pumped to the desulphurization circulating pump discharge, flue gas in thionizer with the doctor solution counter current contact, remove SO
2Flue gas drained in the atmosphere by the desulfurization cat head, control doctor solution pH value 6.2.Ammonium sulfate liquor moisture is evaporated the generation crystallization in evaporative crystallizer, contains the ammonium sulfate liquor of crystallization through being pumped to sulphur crystalline ammonium device fractional crystallization, and ammonium sulfate liquor returns thionizer.
Claims (2)
1. one kind is the equipment of raw material production sulphur ammonium with sulphur slurry and ammoniacal liquor, it is characterized in that, comprises roasting kiln, waste heat boiler, evaporative crystallizer, mother liquor well heater, water cooler, thionizer, ammonium sulfate liquor groove; The roasting kiln outlet is connected by exhaust gases passes with waste heat boiler, the waste heat boiler outlet links to each other with evaporative crystallizer by exhaust gases passes, evaporative crystallizer links to each other with the mother liquor well heater by recycle pump, the mother liquor heater outlet links to each other with evaporative crystallizer internal upper part shower nozzle by pipeline, the evaporative crystallizer top exit is connected with water cooler by blower fan, and cooler outlet is connected with the thionizer bottom; Thionizer middle part and top doctor solution pipe are provided with ammonia inlet, and the thionizer bottom communicates with the ammonium sulfate liquor groove by overflow ducts, and the ammonium sulfate liquor groove is connected with evaporative crystallizer by the connecting tube of ammonium sulfate liquor pump; The evaporative crystallizer bottom is provided with the ammonium sulfate liquor outlet that contains crystallization, is connected with sulphur crystalline ammonium device.
2. according to claim 1 is the equipment of raw material production sulphur ammonium with sulphur slurry and ammoniacal liquor, it is characterized in that described thionizer is two sections, and hypomere is empty spray section, and epimere is packing section, and thionizer top is provided with pounces on the mist layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220680333XU CN203033778U (en) | 2012-12-10 | 2012-12-10 | Device for producing ammonium sulfate by using sulfate pulp and ammonia water as raw materials |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220680333XU CN203033778U (en) | 2012-12-10 | 2012-12-10 | Device for producing ammonium sulfate by using sulfate pulp and ammonia water as raw materials |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203033778U true CN203033778U (en) | 2013-07-03 |
Family
ID=48685915
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201220680333XU Expired - Lifetime CN203033778U (en) | 2012-12-10 | 2012-12-10 | Device for producing ammonium sulfate by using sulfate pulp and ammonia water as raw materials |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203033778U (en) |
Cited By (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 |
| CN103408083A (en) * | 2013-07-31 | 2013-11-27 | 张卫东 | Method for processing ammonia water remaining in coke oven through vacuum flash evaporation method |
| CN104909341A (en) * | 2015-05-19 | 2015-09-16 | 宁波科新化工工程技术有限公司 | Gas desulfurization sulfur slurry concentration process method |
| CN109517630A (en) * | 2019-01-08 | 2019-03-26 | 大连市昊通环保工程技术有限公司 | Coke-stove gas sulfurous acid ammonium salt process deamination produces thiamine process and system |
-
2012
- 2012-12-10 CN CN201220680333XU patent/CN203033778U/en not_active Expired - Lifetime
Cited By (7)
| 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 |
| CN102951657B (en) * | 2012-12-10 | 2014-06-04 | 张卫东 | Process and equipment for producing ammonium sulfate by taking sulfur pulp and ammonia water as raw materials |
| CN103408083A (en) * | 2013-07-31 | 2013-11-27 | 张卫东 | Method for processing ammonia water remaining in coke oven through vacuum flash evaporation method |
| CN103408083B (en) * | 2013-07-31 | 2014-07-23 | 张卫东 | Method for processing ammonia water remaining in coke oven through vacuum flash evaporation method |
| CN104909341A (en) * | 2015-05-19 | 2015-09-16 | 宁波科新化工工程技术有限公司 | Gas desulfurization sulfur slurry concentration process method |
| CN109517630A (en) * | 2019-01-08 | 2019-03-26 | 大连市昊通环保工程技术有限公司 | Coke-stove gas sulfurous acid ammonium salt process deamination produces thiamine process and system |
| CN109517630B (en) * | 2019-01-08 | 2024-06-11 | 大连昊通节能环保工程技术有限公司 | Process and system for producing ammonium sulfate by deammoniation of coke oven gas using ammonium sulfite |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20130703 Effective date of abandoning: 20140604 |
|
| RGAV | Abandon patent right to avoid regrant |