CN103523844A - Ammonia stilling system and process - Google Patents
Ammonia stilling system and process Download PDFInfo
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- CN103523844A CN103523844A CN201310533011.1A CN201310533011A CN103523844A CN 103523844 A CN103523844 A CN 103523844A CN 201310533011 A CN201310533011 A CN 201310533011A CN 103523844 A CN103523844 A CN 103523844A
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Abstract
The invention provides an ammonia stilling process which comprises the following steps: the first step is heating of raw materials, wherein ammonia water in an ammonia water tank conducts heat exchange with hot wastewater discharged from the bottom of an ammonia stilling tower through a rich and poor liquid heat exchanger, and then the ammonia water is injected into a tube furnace convection section to be heated; the second step is a deacidification reaction, wherein lye which is diluted and heated is led out of a lye tank and injected into a deacidification tower, the heated ammonia water is led out of the tube furnace convection section and injected into the deacidification tower for the deacidification reaction, ammonia gas in removed acid gas is recovered through an ammonia gas backflow mechanism, and the remaining acid gas is recovered through an acid gas recoverer; the third step is an ammonia stilling reaction, wherein a residue is led out of the bottom of the deacidification tower and fed into the middle portion of the ammonia stilling tower, and the pressure in the ammonia stilling tower is constant negative pressure; the wastewater at the bottom of the ammonia stilling tower is injected into a tube furnace radiation section to be heated before being returned to the lower portion of a tripping section of the ammonia stilling tower, and the wastewater is used for providing heat needed for ammonia stilling; the removed ammonia gas is fed into an ammonia gas recovery mechanism to be recovered from the top of the ammonia stilling tower. By means of the ammonia stilling process, equipment corrosion can be effectively lowered, recovery efficiency is improved, meanwhile, emission of polluting gases is not caused, and energy conservation and environmental protection are facilitated.
Description
Technical field
The present invention relates to a kind of chemical industry equipment and technology, be specifically related to a kind of ammonia steaming system and technique.
Background technology
In coke-oven plant's remained ammonia, the recovery of ammonia plays a very important role.Ammonia in recovery remained ammonia, the ammonia in rich ammoniacal liquor not only can be produced various nitrogenous fertilizer, more can play the requirement of reduction of discharging and protection of the environment.At present, in remained ammonia, the recovery method of ammonia has: steam direct distillation, tube oven method, heat conduction oil process, negative pressure ammonia still process method and tubular furnace negative pressure ammonia still process method.
But, in the method for these ammonia still processs, all do not consider sulfide in the ammoniacal liquor corrupting influence to ammonia distillation process equipment.In addition, do not consider the impact of sour gas on the purity of the ammonia removing yet.
Summary of the invention
For above-mentioned existing problem, the object of this invention is to provide a kind of ammonia distillation process and system, can reduce technique corrosion, improve the efficiency that ammoniacal liquor reclaims, and the raising ammoniacal liquor that reclaims obtains concentration.
For reaching above-mentioned technique effect, the technical solution used in the present invention is: a kind of ammonia distillation process, comprise the following steps: 1) heating raw materials: the thermal wastewater that the ammoniacal liquor in ammonia vessel is discharged at the bottom of poor rich liquid heat exchanger and ammonia still carries out heat exchange, pass into again afterwards the heating of tube furnace convection zone; 2) depickling reaction: the alkali lye that lye vat is drawn after dilution is heated passes into extracting tower, tube furnace convection zone is drawn ammoniacal liquor after heating and is passed into extracting tower and carry out depickling reaction; Ammonia in the sour gas removing reclaims by ammonia backflow mechanism, and remaining sour gas reclaims by sour gas withdrawer; 3) ammonia still process reaction: draw still liquid at the bottom of extracting tower tower and send into the middle part that tower internal pressure is the ammonia still of permanent negative pressure; After being passed into the heating of tube furnace radiation section, waste water at the bottom of ammonia still tower leads to go back to ammonia still stripping section bottom, in order to ammonia still process institute heat requirement to be provided; The ammonia removing is sent into Ammonia recovery mechanism and is reclaimed from ammonia still top, the thermal wastewater of ammonia still bottom passes into poor rich liquid heat exchanger to carry out carrying out wastewater treatment after heat exchange.
Further, during the ammonia of described ammonia backflow mechanism in reclaiming sour gas, first by sour gas condenser by gas cooling in extracting tower, by sprinker, spray the ammonia in ammonia absorption sour gas afterwards.
Further, the pressure in described extracting tower is normal pressure; In described extracting tower, temperature is at 95 ℃～100 ℃.
Further, the pressure in described ammonia still is-30kp～-27kp; Temperature in described ammonia still is at 135 ℃～145 ℃.
Further, described tube furnace radiation section heating ammoniacal liquor passes into ammonia still again by evaporator evaporation vaporization; Heat required in described ammonia still is all provided by the steam evaporating after the heating of tube furnace radiation section.
The present invention also provides a kind of ammonia steaming system, mainly comprises ammonia vessel, poor rich liquid heat exchanger, tube furnace, extracting tower, ammonia still, Ammonia recovery mechanism, ammonia backflow mechanism, lye vat; The ammonia vessel that stores ammoniacal liquor is connected to the poor rich liquid heat exchanger for heat exchange, and poor rich liquid heat exchanger connects tube furnace, and tube furnace connects extracting tower middle part; Extracting tower top is connected with ammonia vessel, and extracting tower top is connected with recycles the sour gas withdrawer of the sour gas remove and for reclaiming the ammonia backflow mechanism of the ammonia of volatilization; Extracting tower bottom is connected with ammonia still middle part, and ammonia still bottom is connected with tube furnace radiation section and forms circulation, and ammonia still top is connected with Ammonia recovery mechanism.
Further, described ammonia backflow mechanism comprises sour gas condenser and sprinker; Described sprinker is connected with spray pump and ammonia vessel.
Further, between described tube furnace radiation section and ammonia still, be connected with vaporizer.
Further, described ammonia still adopts slant-hole tray.
Further, described Ammonia recovery mechanism comprises complete condenser, not condenser water cooler, vacuum system, ammoniacal liquor backflash; Described ammonia still bottom is also connected with the poor rich liquid heat exchanger of heating ammoniacal liquor.
Further, described Ammonia recovery mechanism comprises complete condenser, not condenser water cooler, vacuum system, ammoniacal liquor backflash; Described ammonia still bottom is also connected with the poor rich liquid heat exchanger of heating ammoniacal liquor.
The invention has the beneficial effects as follows: preposition deacidification equipment before ammonia still process, effectively reduce the corrosion of sour gas to ammonia still process equipment, extended the life-span of relevant device.In extracting tower, install ammonia reflux additional, guaranteed the rate of recovery of ammoniacal liquor, improved the concentration of the ammoniacal liquor reclaiming.By rational pressure and temperature, control, can effectively realize energy saving and cost lowering.In addition, by using vaporizer, effectively reduce the vibrations of equipment, extended equipment life; By adopting slant-hole tray, improved ammonia still process efficiency, also have in addition the advantages such as pressure drop is little, anti-obstruction.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of ammonia distillation process of the present invention and system;
Wherein: 1, remained ammonia groove; 2, remained ammonia pump; 3, porcelain filter; 4, ammonia vessel; 5, spray pump; 6, aqua ammonia pump; 7, gaseous effluent cooler; 8, poor rich liquid heat exchanger; 9, lye vat; 10, volume pump; 11, extracting tower; 12, feeding pump; 13, tube furnace; 14, recycle pump; 15, vaporizer; 16, waste water medial launder; 17, ammonia still; 18, waste water pump; 19, complete condenser; 20, non-condensable gas water cooler; 21, vacuum system; 22, ammoniacal liquor backflash; 23, ammonia backflow mechanism; 24, sour gas condenser; 25, sprinker; 26， Ammonia recovery mechanism; 27, sour gas withdrawer.
Embodiment
Below in conjunction with accompanying drawing, the invention will be further described.
As shown in Figure 1, ammonia steaming system of the present invention mainly comprises ammonia vessel 4, poor rich liquid heat exchanger 8, tube furnace 13, extracting tower 11, ammonia still 17, Ammonia recovery mechanism 26, ammonia backflow mechanism 23.
Remained ammonia from condenser system passes into ammonia vessel 4 by remained ammonia pump 2 through porcelain filter 3 from remained ammonia groove 1; Rich ammoniacal liquor from washing ammonia system is passed into ammonia vessel 4.Ammonia vessel 4 is connected with poor rich liquid heat exchanger 8 by aqua ammonia pump 6, ammoniacal liquor in ammonia vessel 4 carries out after heat exchange with the thermal wastewater at 17 ends of ammonia still in poor rich liquid heat exchanger 8, the convection zone that passes into tube furnace 13 further heats, and passes into afterwards the middle part of extracting tower 11 from tube furnace 13.Top at extracting tower 11 is also connected with lye vat 9, in order to pass into the alkali lye after dilution is heated.
Extracting tower 11 tops are connected with the ammonia backflow mechanism 23 that mainly comprises sour gas condenser 24 and sprinker 25.Sour gas condenser 24 can cool the mixed gas of the sour gas removing in extracting tower 11 and ammonia, passes into absorption liquid simultaneously and absorbs the ammonia in steam, to realize the lost object that reduces ammonia by sprinker 25.Wherein, the absorption liquid in the sprinker 25 at extracting tower 11 tops can be the ammoniacal liquor of the low temperature that obtains through spray pump 5 pressurization from ammonia vessel 4.Meanwhile, ammonia backflow mechanism 23 only comprises sprinker 25, sprays ammoniacal liquor reach the lost object of minimizing ammonia by sprinker 25.Extracting tower 11 tops are also connected with sour gas withdrawer 27, in order to recycle the sour gas of discharging.
The bottom of extracting tower 11 is connected with the middle part of ammonia still 17 through feeding pump 12.The bottom of ammonia still 17 is connected with the radiation section of tube furnace 13 through waste water medial launder 16 and recycle pump 14.At the bottom of the radiation section heating tower of tube furnace 13, after ammoniacal liquor, pass into and in vaporizer 15, after steam raising, pass into ammonia still 17 stripping sections.By using vaporizer 15, can effectively reduce water hammer, reduce the vibrations of equipment, improve the weather resistance of equipment.
The 26， of the Ammonia recovery mechanism Ammonia recovery mechanism 26 that the top of ammonia still 17 is connected with to reclaim tower top ammonia mainly comprises tower top dephlegmator, complete condenser 19, vacuum system 21 and ammoniacal liquor backflash 22.At the bottom of ammonia still 17 towers, be connected with waste water pump 18 with waste water medial launder 16 with poor rich liquid heat exchanger 8, the ammoniacal liquor of extracting out from ammonia vessel 4 in order to heating is lowered the temperature to waste liquid simultaneously.Poor rich liquid heat exchanger 8 is connected with gaseous effluent cooler 7, after low-temperature wastewater after gaseous effluent cooler 7 cools is cooling, sends ammonia and biochemical system to laundry.What ammonia still 17 inside adopted is slant-hole tray, has the advantages such as ammonia still process efficiency is high, pressure drop is little, anti-obstruction.
Below, the main process of description ammonia distillation process.Remained ammonia from condenser system passes through remained ammonia pump 2 through the laggard ammonia vessel 4 of porcelain filter 3 oil removing from remained ammonia groove 1, from the rich ammoniacal liquor of the normal temperature of washing ammonia system, sends into ammonia vessel 4.Ammoniacal liquor in ammonia vessel 4 adds and compresses into poor rich liquid heat exchanger 8 heat exchange to 60 ℃ to 70 ℃ of left and right through aqua ammonia pump 6, then after tube furnace 13 convection zones are heated to 95 ℃ to 100 ℃ left and right, from extracting tower 11 middle parts, adds.The alkali lye of heating from lye vat 9 extraction dilutions adds extracting tower 11 tops by volume pump 10.Extracting tower 11, by the steam heater supplying heat at the bottom of tower, keeps temperature in tower to maintain 95 ℃ to 100 ℃, and optimum is 98 ℃ of left and right.
At this, the volatility ammonium salt in ammoniacal liquor is heated decomposition, most CO as volatile salt, ammonium sulfide, hydrogenation ammonia etc.
2, H
2s, NH
3, the aobvious gaseous state of HCN overflows from extracting tower 11, for reducing ammonia, with above-mentioned gas, takes away, need to be by the ammonia ammonia that mechanism 23 reclaims wherein that refluxes.Be mainly by steam process sour gas condenser 24 refrigeration cycle in extracting tower 11, reduce the temperature of steam; By spray pump 5, pass into ammoniacal liquor again, absorb ammonia wherein.Because various gas solubilities are different, ammonia major part is absorbed liquid and optionally absorbs; And passing into sour gas withdrawer 27, recycles the sour gas of remaining tower top.
At the bottom of the tower of extracting tower 11, still liquid adds from the middle part of ammonia still 17 through feeding pump 12 pressurizations.Maintain pressure in ammonia still 17 at-30kp～-27kp, divide thermal wastewater to enter waste water medial launder 16 ammonia still 17 bottoms, through recycle pump 14, add force feed tube furnace 13 radiation sections and be heated to 135 ℃～145 ℃, through automatically regulating laggard vaporizer 15, recycling waste water steam raising in vaporizer 15, hot steam is discharged and is entered ammonia still 17 stripping section bottoms by top, and recycling waste water, from flowing into waste water medial launder 16, completes a circulation.At the bottom of ammonia still 17 towers, the waste water of waste water and waste water medial launder 16 adds force feed poor rich liquid heat exchanger 8 through waste water pump 18, and temperature is down to 60～65 ℃ by 85～105 ℃, then is down to after approaching normal temperature and sends ammonia and biochemical system to laundry with the water at low temperature cooling temperature of gaseous effluent cooler 7.The interior needed heat of ammonia still 17 is all provided by the heating of tube furnace radiation section, without extra steam is provided, has greatly simplified technical process, has reduced cost.
The ammonia of ammonia still 17 tower tops enters the cooling adjusting of tower top dephlegmator and refluxes, ammonia is cooled to strong aqua through complete condenser 19 and flows into ammoniacal liquor backflash 22 afterwards, after part non-condensable gas is further cooling by non-condensable gas water cooler 20 again, by vacuum system 21, send into before gas blower in coke-oven coal tracheae, the small part ammoniacal liquor under condensation is got back to ammoniacal liquor backflash 22.
The foregoing is only preferred embodiment of the present invention, in order to limit the present invention, within the spirit and principles in the present invention not all, any modification of making, be equal to replacement, improvement etc., within all should being included in the scope of protection of the invention.
Claims (10)
1. an ammonia distillation process, is characterized in that, comprises the following steps:
1) heating raw materials: the thermal wastewater that the ammoniacal liquor in ammonia vessel is discharged at the bottom of poor rich liquid heat exchanger and ammonia still carries out heat exchange, passes into the heating of tube furnace convection zone afterwards again;
2) depickling reaction: the alkali lye that lye vat is drawn after dilution is heated passes into extracting tower, tube furnace convection zone is drawn ammoniacal liquor after heating and is passed into extracting tower and carry out depickling reaction; Ammonia in the gas removing reclaims by ammonia backflow mechanism, and remaining sour gas reclaims by sour gas withdrawer;
3) ammonia still process reaction: draw still liquid at the bottom of extracting tower tower and send into the middle part that tower internal pressure is the ammonia still of permanent negative pressure; After being passed into the heating of tube furnace radiation section, waste water at the bottom of ammonia still tower leads to go back to ammonia still stripping section bottom, in order to ammonia still process institute heat requirement to be provided; The ammonia removing is sent into Ammonia recovery mechanism and is reclaimed from ammonia still top, the thermal wastewater of ammonia still bottom passes into poor rich liquid heat exchanger to carry out carrying out wastewater treatment after heat exchange.
2. ammonia distillation process according to claim 1, it is characterized in that, during the ammonia of described ammonia backflow mechanism in reclaiming sour gas, first by sour gas condenser by gas cooling in extracting tower, by sprinker, spray the ammonia in ammonia absorption sour gas afterwards.
3. ammonia distillation process according to claim 1, is characterized in that, the pressure in described extracting tower is normal pressure; In described extracting tower, temperature is at 95 ℃～100 ℃.
4. ammonia distillation process according to claim 1, is characterized in that, the pressure in described ammonia still is-30kp～-27kp; Temperature in described ammonia still is at 135 ℃～145 ℃.
5. ammonia distillation process according to claim 1, is characterized in that, described tube furnace radiation section heating ammoniacal liquor passes into ammonia still again by evaporator evaporation vaporization; The steam that in described ammonia still, required heat evaporates after being heated by tube furnace radiation section provides.
6. an ammonia steaming system, is characterized in that, mainly comprises ammonia vessel, poor rich liquid heat exchanger, tube furnace, extracting tower, ammonia still, Ammonia recovery mechanism, ammonia backflow mechanism, lye vat;
The ammonia vessel that stores ammoniacal liquor is connected to the poor rich liquid heat exchanger for heat exchange, and poor rich liquid heat exchanger connects tube furnace, and tube furnace connects extracting tower middle part; Extracting tower top is connected with ammonia vessel, and extracting tower top is connected with recycles the sour gas withdrawer of the sour gas remove and for reclaiming the ammonia backflow mechanism of the ammonia of volatilization;
Extracting tower bottom is connected with ammonia still middle part, and ammonia still bottom is connected with tube furnace radiation section and forms circulation, and ammonia still top is connected with Ammonia recovery mechanism.
7. ammonia steaming system according to claim 6, is characterized in that, described ammonia backflow mechanism comprises sour gas condenser and sprinker; Described sprinker is connected with spray pump and ammonia vessel.
8. ammonia steaming system according to claim 6, is characterized in that, between described tube furnace radiation section and ammonia still, is connected with vaporizer.
9. ammonia steaming system according to claim 6, is characterized in that, described ammonia still adopts slant-hole tray.
10. ammonia steaming system according to claim 6, is characterized in that, described Ammonia recovery mechanism comprises complete condenser, not condenser water cooler, vacuum system, ammoniacal liquor backflash; Described ammonia still bottom is also connected with the poor rich liquid heat exchanger of heating ammoniacal liquor.
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Cited By (9)
| 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 |
| CN103964473A (en) * | 2014-02-25 | 2014-08-06 | 中盐安徽红四方股份有限公司 | Method for preparing alkali by utilizing acid gas in transformation stripping tower of ammonia synthesis device |
| CN105884106A (en) * | 2016-04-22 | 2016-08-24 | 唐山旭阳化工有限公司 | Benzene hydrogenation wastewater desulfurization and deamination treatment method aiming at improving deamination and treatment device applying same |
| CN108384582A (en) * | 2018-02-22 | 2018-08-10 | 中冶焦耐(大连)工程技术有限公司 | A kind of system and technique for strengthening deacidifion desorption |
| CN109704366A (en) * | 2019-02-11 | 2019-05-03 | 中冶焦耐(大连)工程技术有限公司 | A kind of technique and system of the coupling of pressurization deacidifion heat |
| CN110330988A (en) * | 2019-07-25 | 2019-10-15 | 内蒙古万众炜业科技环保股份公司 | A kind of wholegrain diameter coal cracking sub-prime utilizes production technology |
| CN111268694A (en) * | 2020-03-10 | 2020-06-12 | 邓守国 | Double-solid ammonia distillation method |
| CN113086991A (en) * | 2021-05-19 | 2021-07-09 | 新疆广汇新能源有限公司 | Oil-containing ammonia gas oil removal process |
| CN113184936A (en) * | 2021-03-25 | 2021-07-30 | 宣化钢铁集团有限责任公司 | Efficient and energy-saving ammonia distillation deacidification system and method for recycling ammonia nitrogen |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103964473A (en) * | 2014-02-25 | 2014-08-06 | 中盐安徽红四方股份有限公司 | Method for preparing alkali by utilizing acid gas in transformation stripping tower of ammonia synthesis device |
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| CN105884106A (en) * | 2016-04-22 | 2016-08-24 | 唐山旭阳化工有限公司 | Benzene hydrogenation wastewater desulfurization and deamination treatment method aiming at improving deamination and treatment device applying same |
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| CN109704366A (en) * | 2019-02-11 | 2019-05-03 | 中冶焦耐(大连)工程技术有限公司 | A kind of technique and system of the coupling of pressurization deacidifion heat |
| CN110330988A (en) * | 2019-07-25 | 2019-10-15 | 内蒙古万众炜业科技环保股份公司 | A kind of wholegrain diameter coal cracking sub-prime utilizes production technology |
| CN111268694A (en) * | 2020-03-10 | 2020-06-12 | 邓守国 | Double-solid ammonia distillation method |
| CN113184936A (en) * | 2021-03-25 | 2021-07-30 | 宣化钢铁集团有限责任公司 | Efficient and energy-saving ammonia distillation deacidification system and method for recycling ammonia nitrogen |
| CN113086991A (en) * | 2021-05-19 | 2021-07-09 | 新疆广汇新能源有限公司 | Oil-containing ammonia gas oil removal process |
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