CN203307083U - Negative pressure ammonia distiller by using raw gas waste heat as heat source - Google Patents
Negative pressure ammonia distiller by using raw gas waste heat as heat source Download PDFInfo
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- CN203307083U CN203307083U CN2013202874504U CN201320287450U CN203307083U CN 203307083 U CN203307083 U CN 203307083U CN 2013202874504 U CN2013202874504 U CN 2013202874504U CN 201320287450 U CN201320287450 U CN 201320287450U CN 203307083 U CN203307083 U CN 203307083U
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- ammonia
- ammonia still
- waste water
- negative pressure
- still
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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
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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
Abstract
The utility model discloses a negative pressure ammonia distiller by using raw gas waste heat as a heat source. The negative pressure ammonia distiller comprises an ammonia distillation tower, a reboiler, a waste water cooler, a partial condenser, an ammonia condensation cooler, a separator, a vacuum pump or an ejector, an ammonia distillation waste water pump, a waste water circulating pump and connecting pipelines, wherein an alkali liquor inlet is formed in the middle of the ammonia distillation tower, the bottom of the ammonia distillation tower is provided with a circulating ammonia distillation waste water outlet, a ammonia distillation waste water outlet and a circulating ammonia distillation waste water inlet, the top of the ammonia distillation tower is connected with the partial condenser, the ammonia condensation cooler, the separator and the vacuum pump or the ejector through a pipeline, the vacuum pump or the ejector is connected with an outgoing device through a pipeline; the bottom of the ammonia distillation tower is connected with the waste water circulating pump and the reboiler through a pipeline, and the bottom of the ammonia distillation tower is further connected with the ammonia distillation waste water pump and the waste water cooler through a pipeline. The negative pressure ammonia distiller disclosed by the utility model has the advantages of small in investment, low in operation cost, economic in energy source, good in ammonia distillation waste water index, and the like.
Description
Technical field
The utility model relates in coking chemical product recovery technology raw gas waste heat its equipment of negative pressure ammonia still process for thermal source that utilizes.
Background technology
At present, the remained ammonia distil process of coking industry has malleation ammonia still process and two kinds of techniques of negative pressure ammonia still process.
The malleation ammonia distillation process mainly contains: 1. take the direct ammonia still process method of steam as thermal source; 2. take coal gas, steam, the heat conduction wet goods indirect ammonia still process method as thermal source.This type of technique is all to operate under 90～110 ℃ of high temperature, because the corrosive mediums such as ammonia, hydrogen sulfide are strong, causes that facility investment is high, recondition expense is high.Malleation ammonia still process all needs to consume primary energy source (as steam, coke-oven gas etc.) in addition, and consumption is larger, and remained ammonia per ton need consume approximately 150～200kg of steam, and running cost is high.
With malleation ammonia still process, compare, the advantage of negative pressure ammonia still process is to have adopted the vacuum method distillation, and service temperature reduces, and corrosive medium reduces, and technique requires significantly to reduce to equipment material.Owing at lower temperature, operating, thereby the required thermal source of ammonia still process can utilize some waste heats to reduce energy consumption.
Raw gas temperature after coke-oven plant's coke-oven gas gas-liquid separator can be 80 ℃ of left and right, generally, utilize recirculated water, water at low temperature section to make it be cooled to certain temperature rough purification after force feed to subsequent processing.In this process, the coal gas heat is not effectively utilized, but also needs to consume a large amount of water coolants.Therefore efficient recovery and utilize the raw gas waste heat for coking industry energy-saving and emission-reduction important in inhibiting.
The negative pressure ammonia distillation process of present stage mainly contains: 1. diamond heating negative pressure ammonia still process method (CN102336415A), 2. utilize stack gas waste heat negative pressure ammonia still process method (CN102602960A), 3. CN102351265A, 4. CN101259967A.
CN102336415A diamond heating negative pressure ammonia still process method, although this technique can be saved certain energy than the malleation ammonia distillation process, still need to consume primary energy source, fails to utilize waste heat.
CN102602960A utilizes stack gas waste heat negative pressure ammonia still process method, this technology utilization be flue gases of cock oven waste heat (high-quality waste heat), service temperature is higher, the investment and running cost higher, fail to utilize raw gas waste heat (low-quality waste heat).
CN102351265A discloses a kind of coking production remained ammonia negative pressure ammonia distillation process and device, the method utilizes doctor solution to spray suction ammonia vapour, and because after dephlegmator, ammonia vapour is without cooling, flow is large, required injection desulfurization flow quantity is large, and facility investment and running cost are high.Simultaneously in ammonia vapour, have large water gaging to enter desulphurization system, cause desulphurization system water imbalance, the desulfurization discharging any waste liquor increases, and finally turns back to again in ammonia steaming system, causes that the ammonia still process load increases, ammonia still process efficiency is low.
CN101259967A discloses a kind of complete processing of coking industry remained ammonia, after in remained ammonia, adding micro-sodium hydroxide, carry out heat exchange at interchanger and waste water, enter through the post-decompression ammonia still of vacuum pump, ammonia volatilization make remained ammonia under negative pressure state in, ammonia vapour, after cooling, is pressed and delivered to next procedure by vacuum pump.This method directly adds sodium hydroxide solution in remained ammonia, in remained ammonia, prussic acid reacts with sodium hydroxide and generates stable cyanogen salt, be difficult to distillation, cause in distilled ammonia wastewater cyanide content high, have a strong impact on follow-up biochemical sewage and process, finally cause externally discharged waste water can not meet national requirements for environmental protection.In addition, the method is sent into condensing water in the mother liquor of sulphur ammonium operation and is recycled, and facts have proved that this will cause the ammonium sulfate liquor variable color, affects sulphur ammonium quality.
In sum, there is defect in the negative pressure ammonia distillation process of present stage at aspects such as UTILIZATION OF VESIDUAL HEAT IN, ammonia still process efficiency, distilled ammonia wastewater indexs, anxious to be resolved.
The utility model content
The purpose of this utility model is to provide that a kind of low equipment investment, running cost are low, save energy, distilled ammonia wastewater index are good utilizes the negative pressure ammonia still process equipment of raw gas waste heat for thermal source.
For achieving the above object, the utility model is achieved through the following technical solutions:
A kind of negative pressure ammonia still process equipment of raw gas waste heat for thermal source that utilizes, comprise ammonia still, reboiler, gaseous effluent cooler, dephlegmator, the ammonia condensing water cooler, separator, vacuum pump or injector, the distilled ammonia wastewater pump, waste water circulation pump and connecting tube, described ammonia still middle part is provided with alkali liquor inlet, at the bottom of the ammonia still tower, be provided with the outlet of circulation distilled ammonia wastewater, distilled ammonia wastewater outlet and circulation distilled ammonia wastewater entrance, the ammonia still tower top is via pipeline and dephlegmator, the ammonia condensing water cooler, separator is connected with vacuum pump or injector, vacuum pump or injector by pipeline with send device outside and be connected, at the bottom of the ammonia still tower, be connected with waste water circulation pump, reboiler via pipeline, also by pipeline, be connected with distilled ammonia wastewater pump, gaseous effluent cooler at the bottom of the ammonia still tower, gaseous effluent cooler again by pipeline with send device outside and be connected.
In described ammonia still, be provided with disconnected tower tray, disconnected tower tray is positioned at and adds top, alkali position, rises in order to the vapour phase of blocking bottom; Disconnected tower tray top and bottom Ta Bi are provided with gas phase communicating pipe, and the ammonia vapour generated after the ammonia distillation of the disconnected tower tray of ammonia still below is imported in the ammonia still of disconnected tower tray top; The disconnected tower tray top of described ammonia still and bottom are provided with liquid phase communicating pipe, and liquid phase communicating pipe can be arranged in ammonia still, or outside ammonia still, ammonia still top ammoniacal liquor water conservancy diversion, to bottom, are continued to distillation.
Described ammonia still also can be with disconnected tower tray, and the ammonia still with disconnected tower tray form is not packing tower or the tray column that meets the utility model processing requirement.
The remarkable advantage such as compared with prior art, the utility model equipment has that low equipment investment, running cost are low, save energy, distilled ammonia wastewater index are good.Concrete characteristics are:
1) low equipment investment: the utility model is to operate under negative pressure, and the operation of equipment temperature is low, and the dielectric corrosion performance descends, and to the requirement reduction of equipment material, facility investment descends and economizes.
2) low, the save energy of running cost: using the raw gas waste heat as the ammonia still process thermal source, do not need other external energy, the raw gas waste heat is turned waste into wealth, obvious energy conservation; Simultaneously, reduced again the recirculated water of follow-up cooling raw gas waste heat and the consumption of water at low temperature, reduced its running cost, killed two birds with one stone, with the obvious advantage.
3) the distilled ammonia wastewater index is good: have higher ammonia still process, decyanation efficiency.The suitable alkali position that adds has guaranteed the indexs such as ammonia nitrogen in the distilled ammonia wastewater and cryanide ion.
The accompanying drawing explanation
Fig. 1 is one-piece construction figure of the present utility model.
Fig. 2 is ammonia still (the built-in liquid phase communicating pipe) structural representation of the disconnected tower tray of the utility model band.
Fig. 3 is ammonia still (the external liquid phase communicating pipe) structural representation of the disconnected tower tray of band of the present utility model.
Fig. 4 is of the present utility model not with the ammonia still structural representation of disconnected tower tray.
Embodiment
Below in conjunction with accompanying drawing, specific embodiment of the utility model is elaborated.
As shown in Figure 1, utilize the raw gas waste heat to comprise ammonia still 1 for the negative pressure ammonia distillation process required equipment of thermal source, reboiler 2, gaseous effluent cooler 3, dephlegmator 4, ammonia condensing water cooler 5, separator 6, vacuum pump or injector 7, distilled ammonia wastewater pump 8, waste water circulation pump 9 and connecting tube, described ammonia still middle part is provided with alkali liquor inlet 10, at the bottom of the ammonia still tower, be provided with circulation distilled ammonia wastewater outlet 11, distilled ammonia wastewater outlet 12 and circulation distilled ammonia wastewater entrance 13, the ammonia still tower top is via pipeline and dephlegmator 4, ammonia condensing water cooler 5, separator 6 is connected with vacuum pump or injector 7, vacuum pump or injector 7 by pipeline with send device outside and be connected, at the bottom of the ammonia still tower, be connected with waste water circulation pump 9, reboiler 2 via pipeline, also by pipeline, be connected with distilled ammonia wastewater pump 8, gaseous effluent cooler 3 at the bottom of the ammonia still tower, gaseous effluent cooler 3 again by pipeline with send device outside and be connected.
Described ammonia still is divided into the disconnected tower tray (Fig. 2, Fig. 3) of band and is not with two kinds of forms of disconnected tower tray (Fig. 4).The ammonia still of the disconnected tower tray of band, disconnected tower tray are positioned at and add top, alkali position, rise in order to the vapour phase of blocking bottom; Disconnected tower tray top and bottom Ta Bi are provided with gas phase communicating pipe 14, and the ammonia vapour generated after the ammonia distillation of the disconnected tower tray of ammonia still below is imported in the ammonia still of disconnected tower tray top; The disconnected tower tray top of described ammonia still and bottom are provided with liquid phase communicating pipe, liquid phase communicating pipe, 15(was shown in Figure 2) can be arranged in ammonia still, liquid phase communicating pipe, 16(was shown in Figure 3) also can be arranged at outside ammonia still, ammonia still top ammoniacal liquor water conservancy diversion, to bottom, is continued to distillation.
Working process of the present utility model is: as shown in Figure 1, the raw material remained ammonia is directly squeezed into ammonia still 1 top, in 55-70 ℃ of temperature and 15-35KPa(absolute pressure) state under, distill, remove free ammonia and other impurity, alkali liquor inlet 10 at ammonia still 1 middle part adds the alkali lye of respective amount, separates the fixed ammonia in remained ammonia.The part distilled ammonia wastewater of ammonia still 1 bottom 55-70 ℃ is extracted out by waste water circulation pump 9, through reboiler 2 and after having absorbed 60-78 ℃ of thermal medium heat exchange of raw gas waste heat, returns to the thermal source of ammonia still 1 as ammonia still process.
The ammonia vapour that ammonia still 1 top is 55-70 out ℃ after dephlegmator 4 is cooling liquid phase as backflow, vapour phase is cooled to 18-60 ℃ through ammonia condensing water cooler 5, cooled liquid-vapor mixture enters separator 6 and carries out gas-liquid separation, wherein non-condensable gases is delivered to the coal gas precooling tower of ammonia absorption unit or ammonia process oxidation sweetening device after with vacuum pump or injector 7, extracting out, and the ammoniacal liquor after separating is delivered to ammonia process oxidation sweetening device doctor solution system, or deliver to coal gas precooling tower.At the bottom of tower, out distilled ammonia wastewater is extracted out by distilled ammonia wastewater pump 8, after gaseous effluent cooler 3 is cooling, sends into waste disposal plant.
This equipment utilization vacuum pump or liquid ejector aspirate the noncondensable gas after the ammonia condensing water cooler, deliver to the coal gas precooling tower of ammonia absorption unit or ammonia process oxidation sweetening device; The ammoniacal liquor that after the ammonia condensing water cooler, condensation is got off is delivered to ammonia process oxidation sweetening device doctor solution system, or delivers to coal gas precooling tower.This method can make the ammonia still process product obtain effective subsequent disposal, again for desulfurizer provides the ammonia source, has maintained ammonia and the water balance of whole gas cleaning system, has guaranteed the normal operation of whole gas cleaning system.
Claims (3)
1. one kind is utilized the negative pressure ammonia still process equipment of raw gas waste heat for thermal source, it is characterized in that, comprise ammonia still, reboiler, gaseous effluent cooler, dephlegmator, the ammonia condensing water cooler, separator, vacuum pump or injector, the distilled ammonia wastewater pump, waste water circulation pump and connecting tube, described ammonia still middle part is provided with alkali liquor inlet, at the bottom of the ammonia still tower, be provided with the outlet of circulation distilled ammonia wastewater, distilled ammonia wastewater outlet and circulation distilled ammonia wastewater entrance, the ammonia still tower top is via pipeline and dephlegmator, the ammonia condensing water cooler, separator is connected with vacuum pump or injector, vacuum pump or injector by pipeline with send device outside and be connected, at the bottom of the ammonia still tower, be connected with waste water circulation pump, reboiler via pipeline, also by pipeline, be connected with distilled ammonia wastewater pump, gaseous effluent cooler at the bottom of the ammonia still tower, gaseous effluent cooler again by pipeline with send device outside and be connected.
2. the negative pressure ammonia still process equipment of raw gas waste heat for thermal source that utilizes according to claim 1, is characterized in that, in described ammonia still, is provided with disconnected tower tray, and the disconnected tower tray risen in order to the vapour phase of blocking bottom is positioned at and adds top, alkali position; Disconnected tower tray top and bottom Ta Bi are provided with gas phase communicating pipe, and gas phase communicating pipe imports in the ammonia still of disconnected tower tray top for the ammonia vapour by generating after the ammonia distillation of the disconnected tower tray of ammonia still below; The disconnected tower tray top of described ammonia still and bottom are provided with liquid phase communicating pipe, and liquid phase communicating pipe can be arranged in ammonia still, or outside ammonia still, ammonia still top ammoniacal liquor water conservancy diversion, to bottom, are continued to distillation.
3. the negative pressure ammonia still process equipment of raw gas waste heat for thermal source that utilizes according to claim 1, is characterized in that, described ammonia still also can be with disconnected tower tray, and the ammonia still with disconnected tower tray form is not packing tower or tray column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013202874504U CN203307083U (en) | 2013-05-21 | 2013-05-21 | Negative pressure ammonia distiller by using raw gas waste heat as heat source |
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| CN2013202874504U CN203307083U (en) | 2013-05-21 | 2013-05-21 | Negative pressure ammonia distiller by using raw gas waste heat as heat source |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN104787825A (en) * | 2015-04-29 | 2015-07-22 | 济南冶金化工设备有限公司 | Waste heat ammonia distillation device and waste heat ammonia distillation method for gas primary cooler |
| CN106673012A (en) * | 2016-11-11 | 2017-05-17 | 中冶焦耐(大连)工程技术有限公司 | Process and device for producing strong ammonia water through negative pressure operation |
| CN106745062A (en) * | 2017-01-23 | 2017-05-31 | 中冶焦耐(大连)工程技术有限公司 | The technique and device of a kind of negative-pressure operation production concentrated ammonia liquor |
-
2013
- 2013-05-21 CN CN2013202874504U patent/CN203307083U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN104787825A (en) * | 2015-04-29 | 2015-07-22 | 济南冶金化工设备有限公司 | Waste heat ammonia distillation device and waste heat ammonia distillation method for gas primary cooler |
| CN106673012A (en) * | 2016-11-11 | 2017-05-17 | 中冶焦耐(大连)工程技术有限公司 | Process and device for producing strong ammonia water through negative pressure operation |
| CN106673012B (en) * | 2016-11-11 | 2019-07-26 | 中冶焦耐(大连)工程技术有限公司 | A kind of technique and device of negative-pressure operation production concentrated ammonia liquor |
| CN106745062A (en) * | 2017-01-23 | 2017-05-31 | 中冶焦耐(大连)工程技术有限公司 | The technique and device of a kind of negative-pressure operation production concentrated ammonia liquor |
| CN106745062B (en) * | 2017-01-23 | 2019-11-15 | 中冶焦耐(大连)工程技术有限公司 | A kind of technique and device of negative-pressure operation production concentrated ammonia liquor |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180912 Address after: 116085 128 high energy street, Qixian Ling high tech Industrial Park, Dalian, Liaoning Patentee after: ACRE COKING & REFRACTORY ENGINEERING CONSULTING CORPORATION (DALIAN), MCC Address before: 116085 128 high energy street, Qixian Ling high tech Industrial Park, Dalian, Liaoning Patentee before: ACRE COKING & REFRACTORY ENGINEERING CONSULTING CORPORATION, MCC |
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| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20131127 |