CN103553172B - Coking residual ammonia water ammonia distillation process equipment and improved method - Google Patents

Coking residual ammonia water ammonia distillation process equipment and improved method Download PDF

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Publication number
CN103553172B
CN103553172B CN201310578282.9A CN201310578282A CN103553172B CN 103553172 B CN103553172 B CN 103553172B CN 201310578282 A CN201310578282 A CN 201310578282A CN 103553172 B CN103553172 B CN 103553172B
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ammonia
steam
tower
reboiler
still
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CN201310578282.9A
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Chinese (zh)
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CN103553172A (en
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张卫东
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张卫东
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    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Abstract

The invention provides coking residual ammonia water ammonia distillation process equipment and an improved method. The improved method is characterized in that ammonia steam containing NH3, H2S, HCN and other components, which are discharged from the top of an ammonia distillation tower, is pressurized by a first-stage heat pump, is fed into an acid pickling tower for pickling, ammonia removing and demisting so as to obtain ammonia-removed secondary steam; medium pressure steam supplemented for ammonia distillation is injected by a steam injector and is mixed with part of the secondary steam, and the mixed steam is guided to the lower part of an ammonia distillation tower and is used for ammonia water ammonia distillation; and part of secondary steam is pressurized by using a second-stage heat pump, is fed into a reboiler and exchanges heat with ammonia distillation wastewater and is used as a hot source of the reboiler for generating steam. Compared with the prior art, the improved method has the beneficial effects that the ammonia steam at the top of the ammonia distillation tower is subjected to adiabatic compression by the first-stage heat pump, so that the temperature and pressure of the ammonia steam are increased, ammonia in the pressurized ammonia steam is removed by an acid pickling method, so that the steam without ammonia can serve as secondary steam to be recycled in the ammonia distillation process, and the consumption of steam required for the residual ammonia water ammonia distillation is reduced.

Description

A kind of coking remained ammonia ammonia distillation process equipment and improving one's methods
Technical field
The present invention relates to the technical field of process coking remained ammonia, particularly relate to a kind of coking remained ammonia ammonia distillation process equipment and improve one's methods.
Background technology
Containing 300 ~ 450g/Nm in the raw gas that process of coking produces 3water vapour.Raw gas is through cyclic ammonia water spraying cooling and coal gas primary cooler cooling, and the water vapour in raw gas enters cyclic ammonia water with coal gas cooling condensation Cheng Shui, and cyclic ammonia water amount also increases thereupon; Deliver to other device outside this partial ammonia water (being referred to as remained ammonia) increased in cyclic ammonia water to process, remove the detrimental impurity such as ammonia in remained ammonia, phenol and COD, processed waste water is outer row after reaching national corresponding wastewater discharge standard.
At present, the remained ammonia ammonia distillation process of coke-oven plant generally adopts steam stripped method to remove NH in remained ammonia 3, H 2the components such as S, HCN, ammonia still process tower top ammonia vapour drains into coal gas system, and at the bottom of ammonia still, distilled ammonia wastewater delivers to biochemical treatment apparatus.What meet subsequent biochemical treatment unit for making distilled ammonia wastewater enters water requirement, and ammoniacal liquor ammonia distillation process needs to consume a large amount of steam.For improving the concentration sending ammonia in ammonia vapour outside, be provided with ammonia vapour dephlegmator and ammonia vapour water cooler at desorb tower top, ammonia vapour makes to send ammonia vapour outside through partial condensation backflow and reaches 15 ~ 18% containing ammonia density.Dephlegmator and ammonia vapour water cooler also need to consume a large amount of recirculated water when condensation ammonia vapour.Coke-oven plant urgently wishes the application of improvement by ammonia distillation process and new technology, realizes the steam consumption quantity reducing ammonia distillation process, reduces remained ammonia processing cost.
Summary of the invention
The object of the present invention is to provide a kind of coking remained ammonia ammonia distillation process equipment and improve one's methods, what ammonia still process tower top was discharged contains NH 3, H 2the ammonia vapour of the components such as S, HCN adds force feed pickling tower acid wash-out ammonia through one-level heat pump, demist obtains deamination secondary steam; The middle pressure steam that ammonia still process supplements is mixed with part secondary steam by steam injector injection, and mixing steam causes ammonia still bottom for ammoniacal liquor ammonia still process; Reboiler and distilled ammonia wastewater heat exchange will be delivered to after part secondary steam high pressure by secondary heat pump (mechanical vapor compressor), produce the thermal source of steam as reboiler.Incoagulability sour gas drains into coal gas system through vacuum pump.Have reduce costs, advantage rational in infrastructure, simple to operate.
For achieving the above object, the present invention realizes by the following technical solutions:
A kind of coking remained ammonia ammonia distillation process equipment, comprise ammonia still, one-level heat pump, pickling tower, deentrainment tower, steam injector, secondary heat pump, reboiler, acid storage, acid cycle pump, washing water pump, it is characterized in that, described ammonia still top output port is connected with pickling tower by one-level heat pump, bottom ammonia still, output terminal is connected by reboiler with input terminus pipeline, reboiler is connected with deentrainment tower pipeline at output by secondary heat pump, steam injector output terminal is connected with ammonia still, pickling top of tower output terminal is connected with deentrainment tower bottom by pipeline, pickling tower bottom output terminal is connected with acid storage, acid storage is connected with pickling tower top by acid cycle pump, deentrainment tower top output port is connected with steam injector by pipeline, be connected with washing water pump bottom deentrainment tower.
Described ammonia still tower top working pressure absolute pressure is between 0.05 ~ 0.15MPa, and at the bottom of ammonia still tower, working pressure is higher than more than tower top pressure 0.02MPa.
The diluted acid of described pickling tower scrubbing ammonia vapour is sulfuric acid or phosphoric acid.
What utilize ammonia still process tower top to discharge contains NH 3, H 2the steam of S, HCN, wherein containing ammonia density is 2 ~ 6%.Ammonia vapour delivers to pickling tower through one-level heat pump adiabatic compression, ammonia vapour removes the ammonia in ammonia vapour at pickling tower through weak acid scrubbing, deamination steam is discharged by tower top as secondary steam after deentrainment tower demist, part secondary steam and the middle pressure steam filled into are mixed by steam injector delivers to ammonia still bottom, part secondary steam again pressurizes through secondary heat pump and delivers to reboiler heating distilled ammonia wastewater, secondary steam is condensed into water and arranges outward in reboiler, incoagulability sour gas is through vacuum pumping to coal gas system, and concrete steps are as follows:
1) enter ammonia still top after remained ammonia and distilled ammonia wastewater heat exchange, the steam that waste water reboiler produces enters by the bottom of tower, and the middle pressure steam filled into enters ammonia still bottom with part secondary steam after steam injector mixes;
2) NH in remained ammonia 3, H 2the components such as S, HCN, are discharged by tower top through steam stripped desorb, and the distilled ammonia wastewater at the bottom of ammonia still is arranged outward through reboiler;
3) NH is contained in the outer ammonia excretion vapour of tower top 3, H 2the components such as S, HCN, ammonia vapour delivers to pickling tower through the pressurization of one-level heat pump, and pickling tower adopts dilute sulphuric acid or dilute phosphoric acid scrubbing ammonia vapour, removes the ammonia in ammonia vapour;
4) deamination steam flutters the acid mist carried secretly in collection steam by deentrainment tower, deentrainment tower is divided into washing section and filler demist section, deamination steam enters by the bottom of tower, discharged by tower top after the washing of washing water pump 10 washing section circulated sprinkling and demist, the deamination steam after deamination, demist is recycled in ammoniacal liquor ammonia still process as secondary steam;
5) ammoniacal liquor ammonia still process needs supplementary a certain amount of middle pressure steam, middle pressure steam sprays through steam injector and mixes with part secondary steam, mixed secondary steam delivers to ammonia still bottom, part secondary steam pressurizes again through secondary heat pump, reboiler and distilled ammonia wastewater indirect heat exchange is delivered to after pressurization, the steam that in reboiler, distilled ammonia wastewater produces enters at the bottom of ammonia still, and secondary steam is condensed into water and arranges outward, and in secondary steam, incoagulability sour gas drains into coal gas system through vacuum pump;
6) the distilled ammonia wastewater heat exchange rear section vaporization in reboiler, the steam of generation enters at the bottom of ammonia still, and the distilled ammonia wastewater that reboiler is discharged is through ammoniacal liquor interchanger and remained ammonia heat exchange.
Compared with prior art, the invention has the beneficial effects as follows:
Ammonia still process tower top ammonia vapour improves the temperature and pressure of ammonia vapour through one-level heat pump adiabatic compression, and the ammonia vapour after pressurization removes ammonia in ammonia vapour through acid wash, makes deamination steam can be used as secondary steam and recycles in ammonia distillation process.Reduce the consumption of steam needed for remained ammonia ammonia still process.
Accompanying drawing explanation
Fig. 1 is structure iron of the present invention.
1-ammonia still 2-one-level heat pump 3-pickling tower 4-deentrainment tower 5-steam injector 6-secondary heat pump 7-reboiler 8-acid storage 9-acid cycle pump 10-washing water pump
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is further illustrated:
As shown in Figure 1, a kind of coking remained ammonia ammonia distillation process equipment, by ammonia still 1, one-level heat pump 2, pickling tower 3, deentrainment tower 4, steam injector 5, secondary heat pump 6, reboiler 7, acid storage 8, acid cycle pump 9 and washing water pump 10 form, ammonia still 1 top output port is connected with pickling tower 3 by one-level heat pump 2, bottom ammonia still 1, output terminal is connected by reboiler 7 with input terminus pipeline, reboiler 7 by secondary heat pump 6 with go out deentrainment tower 4 pipeline at output and be connected, steam injector 5 output terminal is connected with ammonia still 1, pickling tower 3 top output port is connected with deentrainment tower 4 bottom by pipeline, bottom pickling tower 3, output terminal is connected with acid storage 8, acid storage 8 is connected with pickling tower 3 top by acid cycle pump 9, deentrainment tower 4 top output port is connected with steam injector 5 by pipeline, be connected with washing water pump 10 bottom deentrainment tower 4.Ammonia still 1 tower top working pressure absolute pressure is between 0.05 ~ 0.15MPa, at the bottom of ammonia still 1 tower, working pressure is higher than more than tower top pressure 0.02MPa, the diluted acid of pickling tower 3 scrubbing ammonia vapour is sulfuric acid or phosphoric acid, the technical process of two kinds of weak acid scrubbing deaminations is identical, and following technical process describes for sulfuric acid.
What utilize ammonia still process tower top to discharge contains NH 3, H 2the ammonia vapour of S, HCN, wherein containing ammonia density is 2 ~ 6%.Ammonia vapour delivers to pickling tower through one-level heat pump (vapour compressor) adiabatic compression.Ammonia vapour removes the ammonia in ammonia vapour at pickling tower through weak acid scrubbing, deamination steam is discharged by tower top as secondary steam after deentrainment tower demist, part secondary steam and the middle pressure steam filled into are mixed by steam injector delivers to ammonia still bottom, and part secondary steam again pressurizes through secondary heat pump and delivers to reboiler heating distilled ammonia wastewater.Secondary steam is condensed into water and arranges outward in reboiler, incoagulability sour gas through vacuum pumping to coal gas system.Its specific operation process is described below:
1) enter ammonia still 1 top after remained ammonia and distilled ammonia wastewater heat exchange, the steam that waste water reboiler 7 produces enters by the bottom of tower, and the middle pressure steam filled into and part secondary steam enter ammonia still 1 bottom after steam injector 5 mixes; ;
2) NH in remained ammonia 3, H 2the components such as S, HCN, are discharged by tower top through steam stripped desorb, and the distilled ammonia wastewater at ammonia still 1 end is arranged outward through reboiler;
3) ammonia still 1 pushes up in outer ammonia excretion vapour containing NH 3, H 2the components such as S, HCN, ammonia vapour delivers to pickling tower 3 through one-level heat pump 2 pressurization, and pickling tower 3 adopts dilute sulphuric acid scrubbing ammonia vapour, removes the ammonia in ammonia vapour;
4) deamination steam flutters the acid mist carried secretly in collection steam by deentrainment tower 4, dilution heat of sulfuric acid in acid storage 8 delivers to pickling tower top spray through acid cycle pump 9, ammonia in dilution heat of sulfuric acid absorbing ammonia vapour generates ammonium sulfate, ammonium sulfate liquor is by draining into acid storage 8 at the bottom of tower, part ammonium sulfate liquor delivers to ammonium sulfate device, and sulfuric acid and water add to acid storage 8.Deentrainment tower is divided into washing section and filler demist section, and deamination steam enters by the bottom of tower, is discharged after the washing of washing section circulated sprinkling and demist by tower top, and the secondary steam part of discharge is mixed into ammonia still 1 bottom through steam injector 5 and the middle pressure steam filled into.Deamination steam after deamination, demist is recycled in ammoniacal liquor ammonia still process as secondary steam;
5) ammoniacal liquor ammonia still process needs supplementary a certain amount of middle pressure steam, middle pressure steam sprays through steam injector and mixes with part secondary steam, mixed secondary steam delivers to ammonia still bottom, part secondary steam pressurizes again through secondary heat pump 6, reboiler 7 and distilled ammonia wastewater indirect heat exchange is delivered to after pressurization, the steam that in reboiler 7, distilled ammonia wastewater produces enters at the bottom of ammonia still, and secondary steam is condensed into water and arranges outward, and in secondary steam, incoagulability sour gas drains into coal gas system through vacuum pump; The steam that steam needed for ammonia still 1 ammonia still process also can all be produced by reboiler 7 supplies at the bottom of tower;
6) the distilled ammonia wastewater heat exchange rear section vaporization in reboiler, the steam of generation enters at the bottom of ammonia still, and the distilled ammonia wastewater that reboiler is discharged is through ammoniacal liquor interchanger and remained ammonia heat exchange.
Ammonia vapour ammonia steam pressure after the pressurization of one-level heat pump is elevated between 1.2 ~ 1.5 times of scopes of original pressure; Deamination secondary steam is after steam injector, and vapor pressure is higher than ammonia still more than bottom pressure 0.02MPa; Deamination secondary steam is after the pressurization of secondary heat pump, and secondary steam temperature of saturation is higher than service temperature at the bottom of ammonia still 10 more than ゜ C; When reboiler duty pressure is higher than coal gas system pressure, can cancel vacuum pump system, the non-condensable gases in reboiler directly drains into coal gas system.
In dilute sulphuric acid liquid absorbing ammonia vapour, ammonia generates ammonium sulfate, and the dilution heat of sulfuric acid of part sulfur-bearing ammonium is delivered to ammonium sulfate device and extracted sulphur ammonium.In dilute phosphoric acid liquid-absorbent ammonia vapour, ammonia generates phosphorus ammonium, and the dilute phosphoric acid solution of the phosphorous ammonium of part delivers to the process of phosphorus ammonium desorption apparatus.

Claims (4)

1. a coking remained ammonia ammonia distillation process equipment, comprise ammonia still, one-level heat pump, pickling tower, deentrainment tower, steam injector, secondary heat pump, reboiler, acid storage, acid cycle pump, washing water pump, it is characterized in that, described ammonia still top output port is connected with pickling tower by one-level heat pump, bottom ammonia still, output terminal is connected by reboiler with input terminus pipeline, reboiler is connected with deentrainment tower pipeline at output by secondary heat pump, steam injector output terminal is connected with ammonia still, pickling top of tower output terminal is connected with deentrainment tower bottom by pipeline, pickling tower bottom output terminal is connected with acid storage, acid storage is connected with pickling tower top by acid cycle pump, deentrainment tower top output port is connected with steam injector by pipeline, be connected with washing water pump bottom deentrainment tower.
2. a kind of coking remained ammonia ammonia distillation process equipment according to claim 1, is characterized in that, described ammonia still tower top working pressure absolute pressure is between 0.05 ~ 0.15MPa, and at the bottom of ammonia still tower, working pressure is higher than more than tower top pressure 0.02MPa.
3. a kind of coking remained ammonia ammonia distillation process equipment according to claim 1, is characterized in that, the diluted acid of described pickling tower scrubbing ammonia vapour is sulfuric acid or phosphoric acid.
4. adopt processing unit according to claim 1 to be used for improving the method for coking remained ammonia ammonia distillation process, be utilize ammonia still process tower top to discharge contain NH 3, H 2the ammonia vapour of S, HCN, wherein containing ammonia density is 2 ~ 6%; Ammonia vapour delivers to pickling tower through one-level heat pump adiabatic compression, ammonia vapour removes the ammonia in ammonia vapour at pickling tower through weak acid scrubbing, deamination steam is discharged by tower top as secondary steam after deentrainment tower demist, part secondary steam and the middle pressure steam filled into are mixed by steam injector delivers to ammonia still bottom, part secondary steam again pressurizes through secondary heat pump and delivers to reboiler heating distilled ammonia wastewater, secondary steam is condensed into water and arranges outward in reboiler, incoagulability sour gas through vacuum pumping to coal gas system, it is characterized in that, concrete steps are as follows:
1) enter ammonia still top after remained ammonia and distilled ammonia wastewater heat exchange, the steam that waste water reboiler produces enters by the bottom of tower, and the middle pressure steam filled into enters ammonia still bottom with part secondary steam after steam injector mixes;
2) NH in remained ammonia 3, H 2s, HCN component, is discharged by tower top through steam stripped desorb, and the distilled ammonia wastewater at the bottom of ammonia still is arranged outward through reboiler;
3) NH is contained in the outer ammonia excretion vapour of ammonia still process tower top 3, H 2s, HCN component, ammonia vapour delivers to pickling tower through the pressurization of one-level heat pump, and pickling tower adopts dilute sulphuric acid or dilute phosphoric acid scrubbing ammonia vapour, removes the ammonia in ammonia vapour;
4) acid mist of deamination steam by carrying secretly in deentrainment tower trapped vapor, deentrainment tower is divided into washing section and filler demist section, deamination steam enters by the bottom of tower, discharged by tower top after the washing of washing water pump washing section circulated sprinkling and demist, the deamination steam after deamination, demist is recycled in ammoniacal liquor ammonia still process as secondary steam;
5) ammoniacal liquor ammonia still process needs supplementary a certain amount of middle pressure steam, and middle pressure steam sprays through steam injector and mixes with part secondary steam, and mixed steam delivers to ammonia still bottom, and part is containing H 2the secondary steam of S, HCN gas pressurizes again through secondary heat pump, reboiler and distilled ammonia wastewater indirect heat exchange is delivered to after pressurization, the steam that in reboiler, distilled ammonia wastewater produces enters at the bottom of ammonia still, secondary steam is condensed into water and arranges outward, and in secondary steam, incoagulability sour gas drains into coal gas system through vacuum pump;
6) the distilled ammonia wastewater heat exchange rear section vaporization in reboiler, the steam of generation enters at the bottom of ammonia still, and the distilled ammonia wastewater that reboiler is discharged is through ammoniacal liquor interchanger and remained ammonia heat exchange.
CN201310578282.9A 2013-11-15 2013-11-15 Coking residual ammonia water ammonia distillation process equipment and improved method CN103553172B (en)

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CN104355321B (en) * 2014-10-23 2016-06-08 中冶焦耐工程技术有限公司 The controlled phosphorus ammonium of product ammonia concn is washed ammonia and is produced strong aqua ammonia technique and device
CN104445476B (en) * 2014-11-25 2017-01-25 江苏和诚制药设备制造有限公司 Ethyl alcohol biogas slurry deamination technology and equipment
CN104743728B (en) * 2015-03-27 2016-08-24 王文领 A kind of energy-saving deamination method of residual coking ammonia water negative pressure deamination
CN104860464B (en) * 2015-05-22 2017-05-03 江西耐可化工设备填料有限公司 Energy-saving ammonia-nitrogen wastewater treatment method and device
CN105481036B (en) * 2015-11-06 2018-02-23 王文领 A kind of residual coking ammonia water energy-saving type negative pressure deamination method
CN105417813B (en) * 2015-11-09 2018-01-26 宁波科新化工工程技术有限公司 A kind of vacuum carbonate desulfuration waste liquid treatment process method
CN106219571B (en) * 2016-09-14 2018-08-21 南京高捷轻工设备有限公司 Evaporate depth recovery system and recovery method that deamination realizes ammonia near-zero release
CN106673014B (en) * 2016-12-29 2018-11-23 天津市创举科技股份有限公司 A kind of coke oven gas desulfurization Study of Deamination is for ammonium hydroxide technique
CN109647160A (en) * 2017-10-12 2019-04-19 宝武炭材料科技有限公司 A method of processing ammonium sulfate liquor circulating slot tail gas

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Publication number Priority date Publication date Assignee Title
SU656976A1 (en) * 1976-10-25 1979-04-15 Украинский научно-исследовательский углехимический институт Method of reprocessing ammonia liquor of byproduct coke industry
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