CN101259967A - Vacuum ammonia distillation technique - Google Patents
Vacuum ammonia distillation technique Download PDFInfo
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- CN101259967A CN101259967A CNA2008100493198A CN200810049319A CN101259967A CN 101259967 A CN101259967 A CN 101259967A CN A2008100493198 A CNA2008100493198 A CN A2008100493198A CN 200810049319 A CN200810049319 A CN 200810049319A CN 101259967 A CN101259967 A CN 101259967A
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- ammonia
- water
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides a manufacturing process for surplus ammonia water in the coal carbonization industry, wherein the surplus ammonia water is added in with sodium hydroxides in minute quantities and exchanges heat with waste water in a heat exchanger, and enters an ammonia still decompressed by a vacuum pump, and the ammonia in the surplus ammonia water is volatilized in a negative pressure state, and the ammonia gases are cooled and sent to a next working procedure after being pressurized by the vacuum pump. The invention is characterized in that the surplus ammonia water is added in with sodium hydroxides so as to decompose and fix ammonium salts; the ammonia still is decompressed by the vacuum pump; the ammonia still is the material filling type ammonia still; and the waste water on the bottom of the ammonia still exchanges heat with the circulating ammonia water and returns to the ammonia still. The invention provides a new way for process technology of surplus ammonia water, and eliminates consumptions of resources such as steam and coal gas, etc. in the process of processing surplus ammonia water, thereby greatly lowering operating costs; moreover, the process of the invention has the advantages of low requirement of the process on the quality of fillers, low pre-stage investment and good economic benefits, and can be used in environments with low temperature and low pressure.
Description
Affiliated technical field
The invention provides a kind of complete processing that is widely used in the coking industry remained ammonia.
Background technology
In the coking production process, produce and contain in a large number that phenol, cyanogen, oil, ammonia nitrogen etc. are poisonous, the remained ammonia of objectionable impurities, mainly from the treating process of coking and gas purification process and Chemicals.Remained ammonia mainly is made up of three parts: the constitution water that the hygroscopic water on shove charge coal surface, the shove charge dry distillation of coal produce and be added into the oil-containing processing wastewater of inhaling in gas line and the effuser circulation oxygen water pump, the remained ammonia total amount is generally by shove charge coal 14%.The conventional machining process of remained ammonia is to utilize steam to carry out direct ammonia still process, this process energy consumption is (1 ton of remained ammonia of every processing need consume about steam 150-200Kg) greatly, corrosion to equipment is also very serious, partial fixing ammonium salt in the remained ammonia can't decompose, make in the waste water ammonium content higher, enter behind the vapor condensation in the distilled ammonia wastewater, increased the load of back road wastewater treatment operation.Though there is utilization tube furnace (thermal oil) heating remained ammonia to reduce the technologic improvement of steam consumption quantity in recent years, consume a large amount of coal gas resources and heat, still do not solve question of substance.
Summary of the invention
The invention provides a kind of new process for processing of coking industry remained ammonia, solved problems such as traditional ammonia distillation process energy consumption height, efficient are low, seriously corroded.
Technical scheme of the present invention is the sodium hydroxide solution that adds trace at remained ammonia, carry out heat exchange through the waste water at the bottom of interchanger and the tower then, enter through the post-decompression ammonia still of vacuum pump, under negative pressure state, make the ammonia volatilization in the remained ammonia, ammonia through the cooling after, by the vacuum pump positive delivery to next procedure.Tower bottom returns at the bottom of the tower after dividing waste water and cyclic ammonia water heat exchange.Its principal character is:
A. in the raw material remained ammonia, add sodium hydroxide solution in order to decompose solid ammonium-salt.Its chemical equation:
(NH
+ 4+OH
-＝NH
3+H
2O)。
B. ammonia still pressure is in vacuum state less than barometric point.
C. the sensible heat that utilizes cyclic ammonia water provides the evaporation thermal source at the bottom of for tower.
D. the ammonia still internal structure is a material filling type.
E. ammonia utilizes vacuum pump pressurization back to carry.
F. condensing water is sent in the mother liquor of sulphur ammonium operation and is utilized.
Processing technique for residual ammonia water of the present invention, saidly in the raw material remained ammonia, add sodium hydroxide solution, be for the solid ammonium-salt that makes remained ammonia is decomposed into volatilization ammonia, thereby reduce the content of ammonia in the waste water effectively, the concentration of sodium hydroxide solution of indication is the scope at 30%-40%; Said ammonia still pressure is less than barometric point, is meant the ammonia still process extraction tower after the vacuum pump decompression, and its tower internal pressure is-77.4～-75.4Kpa, be in vacuum state; Said ammonia still process extraction tower internal structure is a material filling type, is meant that this ammonia still process complete processing moves under low temperature, low pressure, has changed the metal tray structure of traditional ammonia still, thereby has reduced equipment investment cost; Said ammonia is carried by vacuum pump pressurization back, is meant that the ammonia that is processed can be according to the requirement of next procedure, and required pressure is carried in adjustment; The said sensible heat that utilizes cyclic ammonia water provides the evaporation thermal source at the bottom of for tower, be meant that the required thermal source of ammonia still process process is provided by the sensible heat of the cyclic ammonia water that is sent to coke oven, waste water is boosted by the pump that boils again at the bottom of the ammonia still, after reboiler and cyclic ammonia water heat exchange intensification, return into the ammonia still bottom, waste water seethes with excitement at the bottom of making tower, thereby has cancelled resource consumptions such as coal gas, steam; Utilize again in the said mother liquor of sending into sulphur ammonium operation after condensing, be meant that tower bottom divides the waste water vaporization after, enter ammonia cooler from cat head, condensing water is sent in the mother liquor of sulphur ammonium operation through the pump pressurization.
The present invention courageously breaks through traditional ammonia distillation process of coking industry, has proposed new technical scheme, has cancelled the consumption of resources such as steam, coal gas, makes original ammonia distillation process running cost height, situation that working (machining) efficiency is low obtain radical change.
Description of drawings
Fig. 1 is the ammonia distillation process general flow chart
Embodiment
Patent of the present invention is implemented by following concrete steps: with treatment capacity per hour is 60m
3Remained ammonia be example: 45 ℃～50 ℃ remained ammonias raw material ammonia tank 1 static with weight separating of oil after, by 2 pressurizations of raw material ammonia water pump, 65 ℃ of waste water sending out with deposed ammonia pump 5 enter the ammonia still top after interchanger 4 heat exchange to 55 ℃～58 ℃, 3 sections fillers are arranged in the ammonia still 6, and ammoniacal liquor is gone into tower and is established liquid distributor.By vacuum pump 12, make to keep vacuum state in the ammonia still, tower top pressure is-77.4KPa that tower bottom pressure is-75.4KPa.Liquid is about 65 ℃ of boilings at the bottom of the tower, the raw material ammonia water that the water vapor that produces and cat head get off contacts in that filling surface is reverse, ammonia in the remained ammonia is resolved to come out, be cooled to 35 ℃-40 ℃ through dephlegmator 10 (using recirculated water), the separation that is condensed of most of steam in the gas, then by vacuum pump with gas after be pressurized to 120Kpa-150Kpa (absolute pressure), be sent to next procedure.(seeing accompanying drawing 1 for details)
Ingress at the raw material ammonia water pump is provided with mixing tank, puts the sodium hydroxide solution that groove 2 adds raw material ammonia water flow 0.8% from the sodium hydroxide height, in order to decompose the solid ammonium-salt in the remained ammonia.The condensing water that is condensed in the cat head gas enters condensing tank 9, and tank inside is provided with built-in fluid-tight, guarantees not to be inhaled into air before the vacuum pump, and the liquid of condensing tank can be regularly or delivered to utilization again in the mother liquor of sulphur ammonium operation with condensate pump 11 continuously.
The required evaporation thermal source of ammonia still is provided by the about 75 ℃ cyclic ammonia water that is sent to coke oven.Waste water is boosted by the pump that boils again (7) at the bottom of the ammonia still,, returns into the ammonia still bottom after being warming up to 68～70 ℃ through reboiler (8) and cyclic ammonia water heat exchange according to the 1100m3/h internal circulating load.
It below is the key technical indexes contrast table of traditional ammonia distillation process and technology of the present invention
| Sequence number | Project | Unit | The tradition ammonia distillation process | Technology of the present invention |
| 1 | The raw material ammonia water yield | m 3/h | 60 | 60 |
| 2 | Wastewater flow rate at the bottom of the tower | m 3/h | 67～69 | 59.7 |
| 3 | Steam consumption quantity | t/h | 9～12 | 0 |
| 4 | The coal gas consumption | m 3/h | 1500～2000 | 0 |
| 5 | Electric consumption | KW/h | 45～50 | 320～370 |
| 6 | The waste water ammonia content | mg/L | ≥300 | ≤30 |
| 7 | The tower internal pressure | KPa | 40～45 | -77.4～-75.4 |
| 8 | Column bottom temperature | ℃ | ≥120 | 65 |
| 9 | Tower top temperature | ℃ | 100～102 | 55～58 |
From above table as can be seen, technology of the present invention is in operation and has fully phased out the consumption of steam and coal gas, running cost is lower, ammonia content is lower in the waste water, can satisfy the requirement of next procedure to the waste water index fully, because this technology is moved under low temperature, low pressure, most equipment can be used carbon steel material, its inner-tower filling material also can use non-metallic fillers, and early investment is lower, has good economy, environmental benefit and promotional value.
Claims (9)
1. the complete processing of a coking industry remained ammonia, its principal character is:
A. in the raw material remained ammonia, add sodium hydroxide solution in order to decompose solid ammonium-salt.
B. ammonia still process extraction tower pressure is in vacuum state less than barometric point.
C. the sensible heat that utilizes cyclic ammonia water provides the evaporation thermal source at the bottom of for tower.
D. the ammonia still internal structure is a material filling type.
E. ammonia utilizes vacuum pump pressurization back to carry.
F. condensing water is sent in the mother liquor of sulphur ammonium operation and is utilized.
2. according to the complete processing of the described remained ammonia of claim 1, it is characterized in that adding in the raw material remained ammonia concentration 30%～40% sodium hydroxide solution and decompose solid ammonium-salt.Its chemical equation: (NH
+ 4OH
-=NH
3+ H
2O).
3. according to the complete processing of the described remained ammonia of claim 1, it is characterized in that utilizing vacuum pump to the ammonia still process extraction tower reduce pressure-75.4kPa～-77.4kPa.
4. according to the complete processing of the described remained ammonia of claim 1, it is characterized in that the cooled condensed liquid of ammonia is sent in the sulphur ammonium operation mother liquor to utilize again.
5. according to claim 1 and 3 described processing technique for residual ammonia water, it is characterized in that ammonia still process extraction tower inside is material filling type, non-tray structure.
6. the complete processing of remained ammonia according to claim 1 is characterized in that its evaporation heat comes from cyclic ammonia water.
7. according to the complete processing of the described remained ammonia of claim 1, it is characterized in that the ammonia that produces after condensing by the vacuum pump positive delivery.
8. according to the complete processing of claim 1,3 and 6 described remained ammonias, it is characterized in that ammonia still works under vacuum, low temperature (＜80 ℃) environment.
9. according to the complete processing of claim 1 and 6 described remained ammonias, it is characterized in that having cancelled in the production run process consumption of resources such as steam, coal gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100493198A CN101259967A (en) | 2008-03-06 | 2008-03-06 | Vacuum ammonia distillation technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100493198A CN101259967A (en) | 2008-03-06 | 2008-03-06 | Vacuum ammonia distillation technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101259967A true CN101259967A (en) | 2008-09-10 |
Family
ID=39960709
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|---|---|---|---|
| CNA2008100493198A Pending CN101259967A (en) | 2008-03-06 | 2008-03-06 | Vacuum ammonia distillation technique |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102107922A (en) * | 2010-12-27 | 2011-06-29 | 林立峰 | Technology and device for treating industrial wastewater |
| CN102241418A (en) * | 2011-05-20 | 2011-11-16 | 新煤化工技术（上海）有限公司 | Negative pressure distillation equipment and method for residual ammonia water |
| CN102336415A (en) * | 2011-06-23 | 2012-02-01 | 上海同特化工科技有限公司 | Tubular furnace negative pressure ammonia distillation process |
| CN102351265A (en) * | 2011-07-07 | 2012-02-15 | 莱芜钢铁股份有限公司 | Negative pressure ammonia distillation process and device for residual ammonia water in coking production |
| CN102557320A (en) * | 2012-01-17 | 2012-07-11 | 佛山市邦普循环科技有限公司 | Method for treating industrial wastewater containing ammonia, nickel, cobalt and sodium sulfate |
| CN103274489A (en) * | 2013-05-21 | 2013-09-04 | 中冶焦耐工程技术有限公司 | Negative-pressure ammonia distillation process and device taking crude gas waste heat as heat source |
| CN103359802A (en) * | 2012-03-28 | 2013-10-23 | 杜惠红 | Method and device for recovering ammonia from nitrochlorobenzene ammonolysis wastewater |
| CN103359862A (en) * | 2012-03-28 | 2013-10-23 | 杜惠红 | Process and system for treating nitrochlorobenzene ammonolysis wastewater |
| CN103570176A (en) * | 2013-11-01 | 2014-02-12 | 安徽金禾实业股份有限公司 | Method and device for processing waste water of chlorination workshop section in production of pyridinium |
| CN103693797A (en) * | 2013-12-31 | 2014-04-02 | 杨立 | Surplus ammonia water treatment process |
| CN104437055A (en) * | 2014-11-25 | 2015-03-25 | 中冶焦耐工程技术有限公司 | Negative-pressure ammonia distillation process and equipment for deaminizing ammonia before vacuum pump |
-
2008
- 2008-03-06 CN CNA2008100493198A patent/CN101259967A/en active Pending
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102107922A (en) * | 2010-12-27 | 2011-06-29 | 林立峰 | Technology and device for treating industrial wastewater |
| CN102241418A (en) * | 2011-05-20 | 2011-11-16 | 新煤化工技术（上海）有限公司 | Negative pressure distillation equipment and method for residual ammonia water |
| CN102336415A (en) * | 2011-06-23 | 2012-02-01 | 上海同特化工科技有限公司 | Tubular furnace negative pressure ammonia distillation process |
| CN102351265A (en) * | 2011-07-07 | 2012-02-15 | 莱芜钢铁股份有限公司 | Negative pressure ammonia distillation process and device for residual ammonia water in coking production |
| CN102351265B (en) * | 2011-07-07 | 2013-04-24 | 山东钢铁股份有限公司 | Negative pressure ammonia distillation process and device for residual ammonia water in coking production |
| CN102557320A (en) * | 2012-01-17 | 2012-07-11 | 佛山市邦普循环科技有限公司 | Method for treating industrial wastewater containing ammonia, nickel, cobalt and sodium sulfate |
| CN103359862A (en) * | 2012-03-28 | 2013-10-23 | 杜惠红 | Process and system for treating nitrochlorobenzene ammonolysis wastewater |
| CN103359802A (en) * | 2012-03-28 | 2013-10-23 | 杜惠红 | Method and device for recovering ammonia from nitrochlorobenzene ammonolysis wastewater |
| CN103274489A (en) * | 2013-05-21 | 2013-09-04 | 中冶焦耐工程技术有限公司 | Negative-pressure ammonia distillation process and device taking crude gas waste heat as heat source |
| CN103570176A (en) * | 2013-11-01 | 2014-02-12 | 安徽金禾实业股份有限公司 | Method and device for processing waste water of chlorination workshop section in production of pyridinium |
| CN103693797A (en) * | 2013-12-31 | 2014-04-02 | 杨立 | Surplus ammonia water treatment process |
| CN103693797B (en) * | 2013-12-31 | 2016-02-10 | 杨立 | A kind of remained ammonia treatment process |
| CN104437055A (en) * | 2014-11-25 | 2015-03-25 | 中冶焦耐工程技术有限公司 | Negative-pressure ammonia distillation process and equipment for deaminizing ammonia before vacuum pump |
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Open date: 20080910 |