CN103570090A - Negative-pressure ammonia stilling system in coking plant and negative-pressure ammonia stilling process method - Google Patents
Negative-pressure ammonia stilling system in coking plant and negative-pressure ammonia stilling process method Download PDFInfo
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- CN103570090A CN103570090A CN201310507129.7A CN201310507129A CN103570090A CN 103570090 A CN103570090 A CN 103570090A CN 201310507129 A CN201310507129 A CN 201310507129A CN 103570090 A CN103570090 A CN 103570090A
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Abstract
The invention relates to a negative-pressure ammonia stilling system and a negative-pressure ammonia stilling process method. A raw material aqua-ammonia pump is connected with the upper part of a negative-pressure ammonia stilling tower through a mixing pipeline; an ammonia dephlegmator is arranged at the top end of the negative-pressure ammonia stilling tower; the ammonia dephlegmator is connected with an ammonia condenser; the lower part of the ammonia condenser is connected with a condensate tank; the condensate tank is connected with a first pipeline through a condensate pump; one side of the ammonia condenser is connected with a vacuum pump; the vacuum pump is connected with a coal gas pipeline; an outlet in the bottom of the negative-pressure ammonia stilling tower is connected with one side of the lower part of a heat exchanger through an ammonia stilling wastewater pump; a circulation ammonia tank is connected with the bottom of the heat exchanger; the upper part of the heat exchanger is directly connected with one side of the negative-pressure ammonia stilling tower; an alkali tank is connected with the mixing pipeline through a metering alkali pump; a cooling water supply tube is respectively connected with the ammonia dephlegmator and the ammonia condenser; a cooling water return tube is respectively connected with the ammonia dephlegmator and the ammonia condenser. The negative-pressure ammonia stilling system which is simple in structure and capable of effectively reducing energy consumption and stably stilling ammonia is provided.
Description
Technical field
The present invention relates to a kind of ammonia-containing water distillation technique, particularly a kind of coke-oven plant negative pressure ammonia evaporation system and processing method thereof.
Background technology
Along with the development of coking industry, energy-saving and environmental protection become two major issues that coking industry faces.China has hundreds of coke-oven plants at present, can give off the ammonia-containing water of tens million of cubes every year, is wherein mainly for remained ammonia.Remained ammonia is a kind of complicated component, concentration is high, toxicity is large, the main sewage effluent of the trade effluent ，Shi coke-oven plant of difficult degradation, and the main component in remained ammonia has NH
3, H
2s, CO
2, HCN, ammonium salt etc.If the remained ammonia to coke-oven plant is dealt with improperly, the ammonia-nitrogen content severe overweight in waste water, can bring serious environmental problem.
Ammonia distillation process is the effective means of remained ammonia Wastewater Pretreatment, can make the ammonia nitrogen concentration of remained ammonia be reduced to about 300mg/L by 3000-4000mg/L level.Traditional ammonia distillation process is adopted by the most of coke-oven plant of live steam reclaiming process ammonia distillation process ，Wei China.At present, steamed ammonia process is faced with a series of problems such as water vapor unit consumption is large, ammonia still process weak effect, process cost is high, equipment corrosion is serious.Energy consumption in ammonia still process process is the major issue that people pay close attention to always, for ammonia distillation process, carries out energy-conservation research, and the research that particularly reduces steam mono-consumption aspect has good practice significance.
Negative pressure ammonia distillation process has good energy-saving effect, can significantly reduce energy consumption, realize " steam zero consumes ", and this technique has ammonia still extent of corrosion little, the advantage of stable operation etc., the main direction that becomes the development of coking industry ammonia distillation process, has a good application prospect.
Summary of the invention
Goal of the invention: in order to solve current live steam reclaiming process ammonia distillation process big energy-consuming, the invention provides a kind of simple in structurely, can effectively reduce energy consumption, stablize the negative pressure ammonia evaporation system of ammonia still process.
A kind of coke-oven plant negative pressure ammonia evaporation system, raw material ammonia tank is connected with raw material ammonia water pump, raw material ammonia water pump is connected with negative pressure ammonia still top through mixing duct, negative pressure ammonia still top is provided with ammonia dephlegmator, ammonia dephlegmator is connected with ammonia condenser, ammonia condenser bottom is connected with condensation liquid bath, condensation liquid bath is connected with the first pipeline by condensate pump, ammonia condenser one side is connected with vacuum pump, vacuum pump is connected with gas line, negative pressure ammonia still tower bottom outlet is connected with interchanger bottom one side through distilled ammonia wastewater pump, oil-circulating ammonia water tank is connected with interchanger bottom, interchanger top is directly connected with negative pressure ammonia still one side, alkali groove is connected with mixing duct through metering alkali pump, water coolant upper hose respectively with ammonia dephlegmator, ammonia condenser is connected, CWR respectively with ammonia dephlegmator, ammonia condenser is connected.
On described distilled ammonia wastewater pump and the pipeline between interchanger, be circumscribed with biochemical waterpipe.
A processing method for coke-oven plant's negative pressure ammonia still process, the incoming stock ammonia vessel of raw material ammonia water, in raw material ammonia tank standing 7.5～8.5 hours, the raw material ammonia water going out from raw material ammonia tank was after the pressurization of raw material ammonia water pump, with 18～22m
3the flow of/h enters negative pressure ammonia still through mixing duct, from negative pressure ammonia still top spray and, at tower top, steam ammonia vapour, at the bottom of tower, form distilled ammonia wastewater, water coolant upper hose is carried water coolant respectively in ammonia dephlegmator and ammonia condenser; The ammonia that negative pressure ammonia still tower top steams is after ammonia dephlegmator, ammonia condenser are cooling, strong aqua enters the condensation liquid bath of normal pressure, through condensate pump pressurization, by pipeline, enter desulfurization workshop section, from ammonia condenser, non-condensable gases out extracts through vacuum pump, send in gas line, the pressure that makes ammonia still process tower top is-80～-74Kpa; Metering alkali pump is that 30% alkali lye is delivered to mixing duct by mass concentration in alkali groove, enters negative pressure ammonia still together with raw material ammonia water is after mixing duct mixes; Distilled ammonia wastewater at the bottom of negative pressure ammonia still tower is after the pressurization of distilled ammonia wastewater pump, with temperature out in oil-circulating ammonia water tank be 75 ℃ of cyclic ammonia waters that derive from coking workshop section, after interchanger heat exchange, enter negative pressure ammonia still, provide ammonia still process required heat, and keep 60 ℃～65 ℃ of tower top temperatures; Distilled ammonia wastewater pumps another part distilled ammonia wastewater coming and drains into biochemical water treatment system by biochemical waterpipe.
Beneficial effect:
1) utilize the waste heat of cyclic ammonia water that ammonia still process institute heat requirement is provided, no longer consume steam, reduced running cost.
2) by add the method for alkali before raw material ammonia water pump, decompose the fixedly ammonium in ammoniacal liquor, reduce the ammonia-nitrogen content in waste water.
3) phlegma can need to go to desulfurization workshop section or enter the cyclic ammonia water pipeline stove that defocuses and spray according to coke-oven plant, and process choice is flexible and varied.
4) service temperature reduces, and has reduced the requirement to equipment material, and negative pressure ammonia still tower body adopts straight carbon steel can meet production requirement, and the main material selection 0Cr18Ni9 of ammonia dephlegmator can meet need of production.
5) reduction of service temperature, makes raw material ammonia water after static oil removing, not need preheating directly to enter column distillation, and technique is simple, has reduced the investment of equipment.
Negative pressure ammonia distillation process of the present invention and the comparison of steamed ammonia process parameter:
Accompanying drawing explanation
Fig. 1 is annexation schematic diagram of the present invention.
Embodiment
Referring to Fig. 1,1 is alkali groove; 2 is metering alkali pump; 3 is raw material ammonia tank; 4 is raw material ammonia water pump; 5 is distilled ammonia wastewater pump; 6 is negative pressure ammonia still; 7 is ammonia dephlegmator; 8 is ammonia condenser; 9 is vacuum pump; 10 is condensation liquid bath; 11 is condensate pump; 12 is interchanger, and 13 is mixing duct; 14 is oil-circulating ammonia water tank; 15 is biochemical waterpipe; 16 is water coolant upper hose; 17 is the first pipeline; 18 is gas line; 19 is CWR.
A kind of coke-oven plant negative pressure ammonia evaporation system, raw material ammonia tank 3 is connected with raw material ammonia water pump 4, raw material ammonia water pump 4 is connected with negative pressure ammonia still 6 tops through mixing duct 13, negative pressure ammonia still 6 tops are provided with ammonia dephlegmator 7, ammonia dephlegmator 7 is connected with ammonia condenser 8, ammonia condenser 8 bottoms are connected with condensation liquid bath 10, condensation liquid bath 10 is connected with the first pipeline 17 by condensate pump 11, ammonia condenser 8 one sides are connected with vacuum pump 9, vacuum pump 9 is connected with gas line 18, negative pressure ammonia still 6 tower bottom outlets are connected with interchanger 12 bottom one sides through distilled ammonia wastewater pump 5, oil-circulating ammonia water tank 14 is connected with interchanger 12 bottoms, interchanger 12 tops are directly connected with negative pressure ammonia still 6 one sides, alkali groove 1 is connected with mixing duct 13 through metering alkali pump 2, water coolant upper hose 16 respectively with ammonia dephlegmator 7, ammonia condenser 8 is connected, CWR 19 respectively with ammonia dephlegmator 7, ammonia condenser 8 is connected.
On described distilled ammonia wastewater pump 5 and the pipeline between interchanger 12, be circumscribed with biochemical waterpipe 15.
A processing method for coke-oven plant's negative pressure ammonia still process, the incoming stock ammonia vessel 3 of raw material ammonia water, in raw material ammonia tank 3 standing 8 hours, the raw material ammonia water going out from raw material ammonia tank 3 was after 4 pressurizations of raw material ammonia water pump, with 20m
3the flow of/h enters negative pressure ammonia still 6 through mixing duct 13, from negative pressure ammonia still 6 tops sprays and, at tower top, steam ammonia vapour, at the bottom of tower, form distilled ammonia wastewater, water coolant upper hose 16 is carried water coolant respectively in ammonia dephlegmator 7 and ammonia condenser 8;
The ammonia vapour that negative pressure ammonia still 6 tower tops steam is after ammonia dephlegmator 7, ammonia condenser 8 are cooling, enter the condensation liquid bath 10 of normal pressure, through condensate pump 11 pressurizations, by the first pipeline 17, enter desulfurization workshop section, from ammonia condenser 8, non-condensable gases out extracts through vacuum pump 9, send in gas line 18, the pressure that makes ammonia still process tower top is-80～-74Kpa;
Metering alkali pump 2 is that 30% alkali lye is delivered to mixing duct 13 by mass concentration in alkali groove 1, enters negative pressure ammonia still 6 together with raw material ammonia water is after mixing duct 13 mixes;
Distilled ammonia wastewater at the bottom of negative pressure ammonia still (6) tower is after 5 pressurizations of distilled ammonia wastewater pump, with temperature out in oil-circulating ammonia water tank 14 be 75 ℃ of cyclic ammonia waters that derive from coking workshop section, after interchanger 12 heat exchange, enter negative pressure ammonia still, provide ammonia still process required heat, and keep 60 ℃～65 ℃ of tower top temperatures; Distilled ammonia wastewater pump 5 another part distilled ammonia wastewater out drains into biochemical water treatment system by biochemical waterpipe 15.
The main material selection 0Cr of described ammonia dephlegmator 7
18ni
9steel is made.
Claims (4)
1.Yi Zhong coke-oven plant negative pressure ammonia evaporation system, it is characterized in that, raw material ammonia tank (3) is connected with raw material ammonia water pump (4), raw material ammonia water pump (4) is connected with negative pressure ammonia still (6) top through mixing duct (13), negative pressure ammonia still (6) top is provided with ammonia dephlegmator (7), ammonia dephlegmator (7) is connected with ammonia condenser (8), ammonia condenser (8) bottom is connected with condensation liquid bath (10), condensation liquid bath (10) is connected with the first pipeline (17) by condensate pump (11), ammonia condenser (8) one sides are connected with vacuum pump (9), vacuum pump (9) is connected with gas line (18), negative pressure ammonia still (6) tower bottom outlet is connected with interchanger (12) bottom one side through distilled ammonia wastewater pump (5), oil-circulating ammonia water tank (14) is connected with interchanger (12) bottom, interchanger (12) top is directly connected with negative pressure ammonia still (6) one sides, alkali groove (1) is connected with mixing duct (13) through metering alkali pump (2), water coolant upper hose (16) respectively with ammonia dephlegmator (7), ammonia condenser (8) is connected, CWR (19) respectively with ammonia dephlegmator (7), ammonia condenser (8) is connected.
2. coke-oven plant according to claim 1 negative pressure ammonia evaporation system, is characterized in that, on described distilled ammonia wastewater pump (5) and the pipeline between interchanger (12), is circumscribed with biochemical waterpipe (15).
The processing method of 3.Yi Zhong coke-oven plant negative pressure ammonia still process, it is characterized in that the incoming stock ammonia vessel of raw material ammonia water (3), in raw material ammonia tank (3) standing 7.5～8.5 hours, the raw material ammonia water going out from raw material ammonia tank (3) is after raw material ammonia water pump (4) pressurization, with 18～22m
3the flow of/h enters negative pressure ammonia still (6) through mixing duct (13), from negative pressure ammonia still (6) top spray and, at tower top, steam ammonia vapour, form distilled ammonia wastewater at the bottom of tower, water coolant upper hose (16) is carried water coolant respectively in ammonia dephlegmator (7) and ammonia condenser (8); The ammonia that negative pressure ammonia still (6) tower top steams is after ammonia dephlegmator (7), ammonia condenser (8) are cooling, enter the condensation liquid bath (10) of normal pressure, through condensate pump (11) pressurization, by the first pipeline (17), enter desulfurization workshop section, from ammonia condenser (8), non-condensable gases out extracts through vacuum pump (9), send in gas line (18), the pressure that makes ammonia still process tower top is-80～-74Kpa; Metering alkali pump (2) is that 30% alkali lye is delivered to mixing duct (13) by mass concentration in alkali groove (1), enters negative pressure ammonia still (6) together with raw material ammonia water is after mixing duct (13) mixes; Distilled ammonia wastewater at the bottom of negative pressure ammonia still (6) tower is after distilled ammonia wastewater pump (5) pressurization, with temperature out in oil-circulating ammonia water tank (14) be 75 ℃ of cyclic ammonia waters that derive from coking workshop section, after interchanger (12) heat exchange, enter negative pressure ammonia still, provide ammonia still process required heat, and keep 60 ℃～65 ℃ of tower top temperatures; Distilled ammonia wastewater pump (5) another part distilled ammonia wastewater out drains into biochemical water treatment system by biochemical waterpipe (15).
4. the processing method of coke-oven plant according to claim 3 negative pressure ammonia still process, is characterized in that, the described main material selection 0Cr of ammonia dephlegmator (7)
18ni
9steel is made.
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Cited By (7)
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| CN103833093A (en) * | 2014-03-26 | 2014-06-04 | 济钢集团有限公司 | Energy-saving and environment-friendly device and technology for producing concentrated ammonia water |
| CN103833049A (en) * | 2014-03-26 | 2014-06-04 | 济钢集团有限公司 | Device and process for stilling ammonia with negative pressure |
| CN104355345A (en) * | 2014-11-28 | 2015-02-18 | 中冶焦耐工程技术有限公司 | Negative-pressure ammonia distillation tower and ammonia distillation method |
| CN108940092A (en) * | 2018-09-25 | 2018-12-07 | 连云港力场创新科技有限公司 | A kind of process with raw material ammonia water production denitration ammonium hydroxide |
| CN110903863A (en) * | 2019-12-23 | 2020-03-24 | 中冶焦耐(大连)工程技术有限公司 | Primary cooling process and device adopting circulating ammonia water for refrigeration |
| CN112079405A (en) * | 2020-09-29 | 2020-12-15 | 湖北江汉石化装备有限公司 | Coking residual ammonia water negative pressure ammonia distillation energy-saving device |
| CN114797132A (en) * | 2022-05-13 | 2022-07-29 | 广东韶钢松山股份有限公司 | Ammonia distillation system |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103833093A (en) * | 2014-03-26 | 2014-06-04 | 济钢集团有限公司 | Energy-saving and environment-friendly device and technology for producing concentrated ammonia water |
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| CN108940092A (en) * | 2018-09-25 | 2018-12-07 | 连云港力场创新科技有限公司 | A kind of process with raw material ammonia water production denitration ammonium hydroxide |
| CN108940092B (en) * | 2018-09-25 | 2024-07-16 | 连云港力场创新科技有限公司 | Process method for producing ammonia water for denitration by using raw material ammonia water |
| CN110903863A (en) * | 2019-12-23 | 2020-03-24 | 中冶焦耐(大连)工程技术有限公司 | Primary cooling process and device adopting circulating ammonia water for refrigeration |
| CN110903863B (en) * | 2019-12-23 | 2024-06-07 | 中冶焦耐(大连)工程技术有限公司 | Primary cooling process and device adopting circulating ammonia water for refrigeration |
| CN112079405A (en) * | 2020-09-29 | 2020-12-15 | 湖北江汉石化装备有限公司 | Coking residual ammonia water negative pressure ammonia distillation energy-saving device |
| CN114797132A (en) * | 2022-05-13 | 2022-07-29 | 广东韶钢松山股份有限公司 | Ammonia distillation system |
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Application publication date: 20140212 |