CN109534569A - Handle method and apparatus for carrying out the method system containing sour ammonia-containing water - Google Patents
Handle method and apparatus for carrying out the method system containing sour ammonia-containing water Download PDFInfo
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- CN109534569A CN109534569A CN201811324849.9A CN201811324849A CN109534569A CN 109534569 A CN109534569 A CN 109534569A CN 201811324849 A CN201811324849 A CN 201811324849A CN 109534569 A CN109534569 A CN 109534569A
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- lime set
- gas
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- sour
- ammonia still
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- Environmental & Geological Engineering (AREA)
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- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
- Degasification And Air Bubble Elimination (AREA)
Abstract
The present invention relates to a kind of method and apparatus for carrying out the method system of the processing containing sour ammonia-containing water.Method of the invention is handled by processes such as lime set flash distillation, depickling and deaminations containing sour ammonia-containing water, change the partial pressure of the dissolved constituent in waste water using inert gas and/or natural gas and utilizes the principle of dissolved constituent volatility and different solubility, realize simple separation and the recycling of acid impurities and alkaline impurities, while obtaining can be with the purification process water of reuse.
Description
Technical field
The present invention relates to a kind of for containing to what is generated in coal chemical industry, petrochemical industry, fine chemistry industry and other industrial process
The method and corresponding device systems that sour ammonia-containing water is handled.
Background technique
In coal chemical technology, since the raw material containing nitrogen enters in coal gasification apparatus during coal gasification course,
Generate and accumulate ammonia in the workshop sections such as gasification installation, a part of ammonia therein can be with buck outlet, but most ammonia can be with
The reuse of process water, reenters in gasification installation.Due to the continuous accumulation of ammonia, contain the ammonia components in the buck of gasification installation
Amount also constantly increases, and the excessively high ammonia-nitrogen content of the buck of outlet causes sewage-treatment plant to be not normally functioning, final to meet
Not environment protection emission requirement.These ammonia components can enter downstream unit such as purification device, and the ammonia in gasification system is caused to accumulate.
Mainly have applied to technique of the removing containing sour ammonia-containing water in Practical Project at present: ammonia still process treatment process, micro- life
Object treatment process, ammonia aeration treatment process, ion-exchange etc..And in coal chemical industry (such as coal oil) industry, full factory is handled at present
(the NH containing acid containing ammonia of device3、H2S、CO2) the technique of waste water be mainly ammonia still process treatment process, use single column gas stripping process,
Stripping processing is carried out with steam, by decompression temperature raising stripping processing, reduces partial pressure of the solution gas in waste water, it will be in waste water
NH3、H2S、CO2Etc. components be stripped off.Tower overhead gas in stripping process send sulfur recovery or fire through heat exchange gas phase obtained after separation
Torch, overhead condensation liquid that overhead condensation gets off are returned in water-coal-slurry coal gasifying process as with slurry with water or are sent to sewage treatment
It stands；The lime set (tower bottom stripping lime set) of stripper tower bottom returns to other process unit reuses.
According to megaton coal oil project practical operation situation, using the stripper overhead condensate liquid of single column gas stripping process
H2S content can exceeded the discharge index of requirement (do not meet SH3099-2000), and Sewage Disposal or thermoelectric device desulfurization system
System will not receive H2S or the exceeded waste water of sulfide content.
Therefore, there is an urgent need for a kind of new method of the processing containing sour ammonia-containing water is developed, pointedly to solve to contain at present
The problem of sour ammonia-containing water treatment process.
Summary of the invention
In order to solve the above technical problems, it is an object of the present invention to provide a kind of method of the processing containing sour ammonia-containing water,
Wherein, the method comprises the following steps:
(1) after sour ammonia-containing water vacuum flashing will be contained, flashed vapour and lime set I are obtained；
(2) use inert gas and/or natural gas as stripping medium in pretreater lime set I obtained by step (1)
Middle carry out air lift, obtains sour gas I and lime set containing ammonia；
(3) it send after merging sour gas I obtained by flashed vapour obtained by step (1) and step (2) to sulfur recovery unit recycling
Reason；
(4) it by the further air lift in ammonia still after exchanging heat of lime set containing ammonia obtained by step (2), obtains sour gas II and coagulates
Liquid II；By a part of gained lime set II after heat exchange heats up and generates gas-liquid two-phase, the ammonia still is recycled back to for described
Lime set containing ammonia carries out air lift, and remaining lime set II is sent after exchanging heat to downstream units processing；
(5) sour gas II obtained by step (4) is carried out gas-liquid separation, obtains sour gas III and lime set after heat exchange cooling
III；Gained sour gas III is sent to sulfur recovery unit processing or is sent to the processing of torch pipe network；Gained lime set III is sent to downstream
Unit is handled.
Method of the invention can be used for handling the ammonia-containing water containing acid generated in various industrial process, typical as locating
Manage the ammonia-containing water containing acid that coal chemical industry process generates.The coal chemical industry process generates typical such as an oxidation containing sour ammonia-containing water
Liquid containing acid cure, sulfur recovery unit lime set etc. after carbon converter unit technique lime set, low-temp methanol wash unit lime set, oil product is processed.
Method of the invention passes through using molten in inert gas (such as nitrogen) or natural gas (such as dry gas) change sewage
The partial pressure of component is solved, and using the principle of dissolved constituent volatility and different solubility, to realize acid impurities and alkalinity
The simple separation of impurity and recycling, and can also further obtain the purification process water of reuse.
It is a further object of the present invention to provide a kind of for implementing above-mentioned method of the processing containing sour ammonia-containing water of the present invention
Device systems, wherein the device systems include:
Lime set flash tank；
Pretreater, the pretreater are connected to the downstream of the lime set flash tank in a manner of being in fluid communication；
Ammonia still, the ammonia still are connected to the downstream of the pretreater in a manner of being in fluid communication；
Ammonia still process tower top cooler, the ammonia still process tower top cooler are connected to the pretreater in a manner of being in fluid communication
The tower top of tower bottom and the ammonia still；
Gas-liquid separator, the gas-liquid separator are connected under the ammonia still process tower top cooler in a manner of being in fluid communication
Trip；
Reboiler, the reboiler are connected to the tower bottom of the ammonia still in a manner of being in fluid communication；
Sulfur recovery unit, the sulfur recovery unit are connected to the lime set flash tank, described pre- in a manner of being in fluid communication
The downstream for the treatment of column and the gas-liquid separator；And
Technique lime set heat exchanger, the technique lime set heat exchanger are connected to the tower of the ammonia still in a manner of being in fluid communication
The tower bottom on top and the pretreater.
Technical solution of the present invention has feature and advantage below:
1) method of the invention can solve the H of the overhead condensation liquid in the projects such as current coal oil2S content is exceeded, solidifying
The problems such as liquefied ammonia too high levels and system ammonia are accumulated, method of the invention can dodge the waste water containing acid containing ammonia by decompression
The processing such as steaming, air lift, ammonia still process, so that acid constituents content therein reduces and reduces the ammon amount in waste water, thus
Qualified recycle-water can be obtained and return it to other process units and recycle.
2) method of the invention uses the double tower gas stripping process of depickling and deamination, well solved containing sour ammonia-containing water because
H2The problem of S content exceeded (not meeting discharge standard as defined in SH 3099-2000) is without being able to satisfy downstream unit requirement, together
When also solve the problems, such as that the ammonia nitrogen accumulation of the condensate liquid (such as lime set II) rich in ammonia components is too fast.
3) method of the invention uses double tower gas stripping process, wherein pretreater uses inert gas and/or natural gas
It carries out air lift, ammonia still and gas stripping has been played using the gas phase in the gas-liquid two-phase after the heating of lime set II, finally to send
H into the waste water in downstream2S (being calculated with wt%) content≤10ppm is met discharge standard as defined in SH 3099-2000 and expired
Foot downstream unit, which receives, to be required；Meanwhile by selecting inert gas (nitrogen) or natural gas (such as dry gas) as pretreatment
The stripping medium of tower can satisfy the calorific value requirement sent to the sour gas of sulfur recovery unit.
Detailed description of the invention
Fig. 1 is the schematic diagram of the process flow of of the invention one illustrative embodiment.
In above-mentioned attached drawing, each appended drawing reference is respectively indicated: 1 lime set flash tank；2 pretreaters；3 ammonia stills；4 ammonia stills
Push up cooler；5 gas-liquid separators；6 steam condensate water distributing cans；7 reboilers；8 technique lime set heat exchangers；9 tower top lime sets pump；10 steam
Ammonia tower lime set pump；11 air lift lime sets pump；001 containing sour ammonia-containing water；The gaseous mixture of 002 flashed vapour and sour gas I；003 is remaining
Lime set II；004 sour gas III；005 lime set III；006 nitrogen；007 natural gas；008 lime set I；009 lime set containing ammonia；010 heat exchange
Lime set containing ammonia afterwards；011 sour gas II；012 high temperature flashed vapour；013 lime set II；Gas-liquid two-phase after 014 lime set II heating；
015 low-pressure steam；016 steam condensate.
Specific embodiment
Following illustrative embodiment is only for explaining the solution of the present invention, and is not intended to any
Mode limits the protection scope of the application.
In the present invention, unless otherwise indicated, term " containing sour ammonia-containing water " refers to that one kind contains NH3、H2S and CO2Etc. waving
The problems such as acidic aqueous solution of hair property light current alkali matter, direct emission will lead to environmental pollution, so having to pass through processing makes to give up
Content of acid gas reaches certain discharge standard in water, meets downstream unit reception and requires to be discharged.
In the present invention, unless otherwise indicated, term " sour gas " refers to containing NH3、H2S and CO2Etc. components gaseous mixture
Body.
In the present invention, unless otherwise indicated, term " high temperature flashed vapour " refer to upstream process (such as carbon monoxide become
Change cell processes) generate exhaust gas.
In the present invention, unless otherwise indicated, term " low-pressure steam " is that finger pressure is 0.4-1.0MPaG and temperature is
150-250 DEG C of saturation or superheated steam.
In one embodiment, the present invention relates to a kind of method of the processing containing sour ammonia-containing water, wherein the method packet
Containing following steps:
(1) after sour ammonia-containing water vacuum flashing will be contained, flashed vapour and lime set I are obtained；
(2) use inert gas and/or natural gas as stripping medium in pretreater lime set I obtained by step (1)
Middle carry out air lift, obtains sour gas I and lime set containing ammonia；
(3) it send after merging sour gas I obtained by flashed vapour obtained by step (1) and step (2) to sulfur recovery unit recycling
Reason；
(4) it by the further air lift in ammonia still after exchanging heat of lime set containing ammonia obtained by step (2), obtains sour gas II and coagulates
Liquid II；By a part of gained lime set II after heat exchange heats up and generates gas-liquid two-phase, the ammonia still is recycled back to for described
Lime set containing ammonia carries out air lift, and remaining lime set II is sent after exchanging heat to downstream units processing；
(5) sour gas II obtained by step (4) is carried out gas-liquid separation, obtains sour gas III and lime set after heat exchange cooling
III；Gained sour gas III is sent to sulfur recovery unit processing or is sent to the processing of torch pipe network；Gained lime set III is sent to downstream
Unit is handled.
In a preferred embodiment, in above-mentioned steps (1), the temperature of the vacuum flashing is 40-120 DEG C, preferably
55-75 DEG C, pressure 0.5-1.0MPaG, preferably 0.6-0.8MPaG.
In a preferred embodiment, in above-mentioned steps (1), the vacuum flashing carries out in lime set flash tank, institute
Stating flashed vapour can obtain from the tank deck of the lime set flash tank, and the lime set I can be obtained from the tank bottom of the lime set flash tank.
In a preferred embodiment, in above-mentioned steps (2), the lime set I is sent to the tower top of the pretreater,
The lime set I and the stripping medium counter current contacting in the tower of the pretreater is set to carry out air lift；Preferably, the air lift
Condition are as follows: 40-120 DEG C of operation temperature, preferably 55-75 DEG C, operating pressure 0.1-0.8MPaG, preferably 0.2-0.4MPaG.
For containing the depickling of sour ammonia-containing water operation, in above-mentioned steps (2), by the tower for controlling the pretreater
The stripping medium dosage at bottom, can make the acidic components in lime set I be desorbed out as far as possible, to guarantee in tower bottom solution
Sour gas H2The steam rate of S component is higher than 90wt%.In addition, with regard to the stripping medium (the inert gas in above-mentioned steps (2)
Body or natural gas) for, the selection of stripping medium works as acidity mainly to send to the calorific value of the sour gas of sulfur recovery unit
When the charging gas calorific value that gas I meets sulfur recovery unit requires, stripping medium may be selected to be inert gas；It is filled when sending to sulfur recovery
When the charging gas calorific value that the sour gas I set is not able to satisfy sulfur recovery unit requires, stripping medium may be selected to be natural gas.Sulfur recovery
Requirement of the device to the gas calorific value of charging is different because of technology producer.In a preferred embodiment, in above-mentioned steps (2), institute
Stating inert gas can be any inert gas low with the reactivity of lime set I, for example including nitrogen, helium, neon, argon
Gas, Krypton, xenon and radon gas, preferably nitrogen.In a preferred embodiment, in above-mentioned steps (2), the natural gas is
Dry gas (that is, natural gas than the hydrocarbon component content of methane weight less than 5%).In a preferred embodiment, in above-mentioned steps
(2) in, the dosage of the stripping medium is 500-2000Nm3/ h, preferably 700-900Nm3/h。
In above-mentioned steps (2), the sour gas I (includes CO2、H2S and a small amount of NH3Deng) can be from the pretreater
Tower top obtain；The lime set containing ammonia can be obtained from the tower bottom of the pretreater, and it is to be desorbed out sour gas that this, which contains ammonia lime set,
Afterwards contain ammonia solution, wherein containing a small amount of H2S, will contain ammonia lime set sent after exchanging heat to (such as can by pump boosting after send to) steam
The tower top of ammonia tower carries out stripping process with deamination.
Mixed gas for the sulfur recovery processing in above-mentioned steps (3), after the flashed vapour and sour gas I merging
When meeting the gas calorific value requirement of sulfur recovery unit, which is sent to sulfur recovery unit processing；When the flashed vapour and acid
Property gas I merge after mixed gas calorific value be unsatisfactory for downstream sulfur recovery unit gas calorific value require when, adjust pretreater in
Stripping medium be natural gas or increase enter pretreater in natural gas flow.
In a preferred embodiment, in above-mentioned steps (4), in operation temperature be 100-150 DEG C and operating pressure is
Air lift is carried out under conditions of 0.1-0.5MPaG.
In a preferred embodiment, in above-mentioned steps (4), the lime set containing ammonia is divided into two parts, a part contains
Ammonia lime set carries out indirect heat exchange through technique lime set heat exchanger and the lime set II, and another part lime set containing ammonia is cold through ammonia still process tower top
But device is changed with the sour gas II, the preferably described sour gas II with the gaseous mixture from extraneous high temperature flashed vapour indirectly
Then this two-part lime set containing ammonia is converged the lime set containing ammonia after being exchanged heat by heat.
In a preferred embodiment, in above-mentioned steps (4), the sour gas II can be obtained from the tower top of the ammonia still
, sour gas II is to mainly contain alkaline gas NH3With aqueous vapor and micro H2The mixture of S.
In a preferred embodiment, in above-mentioned step (4), the lime set II can be obtained from the tower bottom of the ammonia still
, it is preferable that use temperature to exchange heat for 150-250 DEG C, preferably 150-180 DEG C of low-pressure steam a part of the lime set II,
Wherein, the low-pressure steam can be pressure and (play for the saturation or superheated steam of 0.4-1.0MPaG, preferably 0.4-0.6MPaG
The effect that lime set II is heated)；It is preferred that the lime set II is warming up to 125-140 DEG C through heat exchange, to generate the gas-liquid
Two-phase.
In further preferred embodiment, in above-mentioned step (4), the gas-liquid two-phase is recycled back to the steaming
Ammonia tower and the counter current contacting of lime set containing ammonia carry out air lift.Preferably, the remaining lime set II is sent after exchanging heat to coal gas
Makeup set in be used as shock chilling medium, or as the recycle-water of full factory, preferably as the reuse of device systems of the present invention
Water.
In further preferred embodiment, the low-pressure steam after heat exchanging carries out gas-liquid separation, solidifying with recovered steam
Liquid (that is, the saturation lime set obtained after exchanging heat by low-pressure steam).In further preferred embodiment, in steam condensate point
Low-pressure steam in water pot after heat exchanging carries out gas-liquid separation.
In a preferred embodiment, in above-mentioned step (5), by the sour gas II through ammonia still process tower top cooler with
Lime set containing ammonia is exchanged heat and is cooled down.In further preferred embodiment, in above-mentioned step (5), by the acidity
Gas II is exchanged heat with lime set containing ammonia through ammonia still process tower top cooler after mixing with the high temperature flashed vapour from the external world and is cooled down.Excellent
In the embodiment of choosing, in above-mentioned step (5), the sour gas II through heat exchange cooling after temperature be 85-145 DEG C, it is excellent
100-135 DEG C is selected, pressure 0.1-0.3MPaG.By rationally control upstream sour gas II heat exchange cooling after temperature and pressure,
To make both to contain micro H in the sour gas III after separation2S, while NH is also controlled well3Containing in the gaseous mixture
Amount.
In a preferred embodiment, in above-mentioned step (5), the sour gas II is carried out in gas-liquid separator
Gas-liquid separation.In a preferred embodiment, in above-mentioned step (5), the sour gas III is in the gas-liquid separator
Top obtains.In a preferred embodiment, in above-mentioned step (5), the sour gas III is that the content of ammonia is
The mixed gas of 10wt%-25wt%.In further preferred embodiment, the sour gas III is individually sent to sulphur and is returned
Receiving apparatus.
The H of the lime set III obtained in above-mentioned step (5)2S content is lower than 10ppm, can meet downstream units
It receives and requires.In a preferred embodiment, in above-mentioned step (5), the lime set III can be sent depending on concrete condition to synthesis
Water treatment unit or thermoelectric device or send to Sewage Disposal is handled.It send to synthesis water treatment unit can be used as and be closed containing acid
The neutralization water of Cheng Shui after adjusting pH value, carries out rectification process to synthetic water；Using lime set III as flue gas in thermoelectric device
Liquid containing ammonia stripping, absorb thermoelectric device flue gas in oxysulfide.
Another embodiment of the present invention is related to a kind of for implementing above-mentioned side of the processing containing sour ammonia-containing water of the present invention
The device systems of method, wherein the device systems include:
Lime set flash tank；
Pretreater, the pretreater are connected to the downstream of the lime set flash tank in a manner of being in fluid communication；
Ammonia still, the ammonia still are connected to the downstream of the pretreater in a manner of being in fluid communication；
Ammonia still process tower top cooler, the ammonia still process tower top cooler are connected to the pretreater in a manner of being in fluid communication
The tower top of tower bottom and the ammonia still；
Gas-liquid separator, the gas-liquid separator are connected under the ammonia still process tower top cooler in a manner of being in fluid communication
Trip；
Reboiler, the reboiler are connected to the tower bottom of the ammonia still in a manner of being in fluid communication；
Sulfur recovery unit, the sulfur recovery unit are connected to the lime set flash tank, described pre- in a manner of being in fluid communication
The downstream for the treatment of column and the gas-liquid separator；And
Technique lime set heat exchanger, the technique lime set heat exchanger are connected to the tower of the ammonia still in a manner of being in fluid communication
The tower bottom on top and the pretreater.
In above equipment system, using the lime set flash tank, to dodging containing sour ammonia-containing water as raw material
Steaming processing, to obtain flashed vapour and lime set I；Using the pretreater by the acidity in the lime set I of lime set flash tank
Gas component desorbs；The ammonia components in the lime set containing ammonia from pretreater are removed using the ammonia still；Using described
Gas-liquid two-phase component of the gas-liquid separator for the sour gas II after the cooling that will exchange heat carries out gas-liquid separation processing；Using above-mentioned
Heat exchanger (including ammonia still process tower top cooler, reboiler and technique lime set heat exchanger) carries out each related streams stock in the device systems
Between heat exchange.
Pretreater of the present invention can have arbitrary conventional type in this field.The conventional type can be typically
For plate column or packed tower pattern.It is preferred that the packed tower pattern includes the packed tower pattern of random packing or structured packing, it is excellent
Pretreater described in selection of land has the packed tower pattern of random packing.
Ammonia still of the present invention has arbitrary conventional type in this field.The conventional type can be typically plate
Formula tower or packed tower pattern.The packed tower pattern includes the packed tower pattern of random packing or structured packing, preferably described
Ammonia still has the packed tower pattern of random packing.
The indirect heat exchanger of any pattern in the prior art can be used in heat exchanger of the present invention.
In a preferred embodiment, the device systems further include steam condensate water distributing can, the steam condensate
Water distributing can is connected to the downstream of the reboiler in a manner of being in fluid communication, with for adjusting the reboiler heat exchange area,
The lime set pressure at equilibrium vapor and reboiler both ends.
In a preferred embodiment, the device systems further include multiple pumps, and the multiple pump is separately positioned on
Between the pretreater and the technique lime set heat exchanger and the ammonia still process tower top cooler, the technique lime set heat exchanger with
Between the ammonia still and downstream of the gas-liquid separator, pump of the pump for each related streams stock in the device systems
It send.
Operational process of the illustrative device systems of the present invention when processing is containing sour ammonia-containing water is as follows:
Sour ammonia-containing water raw material will be contained and (such as wash ammonium hydroxide and containing from CO converter unit from what low-temp methanol washed unit
The sour mixed waste water of lime set containing ammonia) it send to lime set flash tank and obtains flashed vapour and lime set I after decompression and flash evaporation.
The lime set I is sent into the tower top of pretreater, gas is carried out to lime set I as stripping medium using nitrogen or dry gas
Processing is proposed, sour gas I and lime set containing ammonia are obtained.
By the sour gas I and the mixed stream stock of flashed vapour from lime set flash tank send together to sulfur recovery unit into
Row recovery processing.
The lime set containing ammonia is divided into two parts after pump boosting, a part is through heat exchanger (such as technique lime set heat exchanger)
Indirect heat exchange is carried out with the part lime set II of the tower bottom from ammonia still, and (such as ammonia still process tower top is cooling through heat exchanger for another part
Device) with the sour gas II of the tower top from ammonia still and the gaseous mixture from extraneous high temperature flashed vapour carries out indirect heat exchange, so
Afterwards, this two parts lime set containing ammonia is convergeed into the lime set containing ammonia after the heat exchange obtained together, the lime set containing ammonia after the heat exchange into
Enter ammonia still and carry out stripping process, obtains sour gas II and lime set II.
The sour gas II is sent out from the tower top of ammonia still, with from extraneous high temperature flashed vapour mix after (by with
Useful object in the exhaust gas that extraneous high temperature flashed vapour mixing further can recycle upstream process to a greater extent
Matter and heat) after heat exchanger (such as ammonia still process tower top cooler) and the cooling of the indirect heat exchange of lime set containing ammonia, it is sent into gas-liquid separator
Gas-liquid separation is carried out, sour gas III and lime set III (H therein are obtained2S content is lower than 10ppm).
The lime set II is sent out from the tower bottom of ammonia still, a portion lime set II through heat exchanger (such as reboiler) with
Low-pressure steam generates gas-liquid two-phase after carrying out indirect heat exchange heating and returns to ammonia still, and ammonia still process tower top is that flows from above to below contains
Ammonia lime set counter current contacting carries out air lift (wherein, the gas phase in gas-fluid two-phase mixture has played actual gas stripping), thus
Air lift is carried out to lime set containing ammonia.It is preferred that the low-pressure steam is sent after heat exchanger (such as reboiler) carries out indirect heat exchange cooling
Gas-liquid separation is carried out to steam condensate water distributing can, thus recovered steam lime set.Remaining lime set II is sent to downstream units and is carried out
Processing typically such as send the recycle-water to coal gasification apparatus as shock chilling medium or as full factory (preferably as this equipment system
The recycle-water of system).
The sour gas III is sent to downstream units and is handled, typically such as send to sulfur recovery unit processing or send to
The processing of torch pipe network.The lime set III is sent to downstream units and is handled, is typically such as sent to synthesis water treatment unit or heat
Electric installation or send to Sewage Disposal is handled.
Embodiment
The materials, reagents and the like used in the following examples is commercially available unless otherwise specified.Following realities
It applies experimental method used in example unless otherwise specified, is conventional method.
1 couple of present invention is further described with reference to the accompanying drawing.
The conduct after washing ammonium hydroxide and mixing containing sour ammonia-containing water from CO converter unit of unit will be washed from low-temp methanol
Raw material (stream stock 001) is sent to lime set flash tank 1, under 0.7MPaG, 65 DEG C of operating condition, after decompression and flash evaporation, is flashed
Gas and lime set I.
The lime set I is sent into the tower top of pretreater 2, nitrogen or day are used under 0.3MPaG, 65 DEG C of operating condition
Right gas gas (requiring and dynamic change with the calorific value of sour gas) carries out stripping process to lime set I as stripping medium, obtains acid
Property gas I and lime set containing ammonia, the dosage of the stripping medium is 800Nm3/h。
The sour gas I and the mixed stream stock 002 of flashed vapour from lime set flash tank 1 are sent together to sulfur recovery list
Member is recycled.The lime set containing ammonia is divided into two parts, a part warp after air lift lime set pump 11 boosts to 0.7MPaG
Technique lime set heat exchanger 8 and the part lime set II of the tower bottom from ammonia still 3 carry out indirect heat exchange, and another part is through ammonia still process tower top
Cooler 4 is changed indirectly with the sour gas II of the tower top from ammonia still 3 and the gaseous mixture from extraneous high temperature flashed vapour
Then this two parts lime set containing ammonia is convergeed to (stream stock 010) together by heat, the lime set containing ammonia that temperature is 115 DEG C after heat exchange enters
Ammonia still 3 carries out stripping process under conditions of operation temperature is 100-150 DEG C and operating pressure is 0.1-0.5MPaG, obtains
Sour gas II and lime set II.
The sour gas II (0.2MPaG, 130 DEG C) is sent out from the tower top of ammonia still 3, is flashed with from extraneous high temperature
After gas (exhaust gas generated by carbon monodixe conversion cell processes, temperature be 150-170 DEG C) mixing through ammonia still process tower top cooler 4 with
Lime set containing ammonia carry out heat exchange be cooled to 100-135 DEG C (pressure 0.1-0.3MPaG) after, be sent into gas-liquid separator 5 carry out gas-liquid
Separation obtains the sour gas III and H that ammonia content is 10wt%-25wt%2S content is lower than the lime set III of 10ppm.
The lime set II is sent out from the tower bottom of ammonia still, a portion lime set is through reboiler 7 and low-pressure steam 015
After (0.5MPaG, 159 DEG C) progress indirect heat exchange is warming up to 125-140 DEG C, generates gas-liquid two-phase and simultaneously return to ammonia still, with ammonia still process
The tower top counter current contacting of lime set containing ammonia that flows from above to below and to lime set containing ammonia carry out air lift.The low-pressure steam 015 is boiled again
Become saturation lime set after the cooling of device indirect heat exchange and be sent to steam condensate water distributing can 6 and carries out gas-liquid separation, recovered steam lime set
016 (0.5MPaG, 159 DEG C of saturation lime set).Remaining lime set II stream stock 003 send to coal gasification apparatus be used as shock chilling medium or
Recycle-water as full factory.
Sour gas III stream stock 004 is sent to sulfur recovery unit or the processing of torch pipe network.By the lime set III (stream stock
005) it send to thermoelectric device or Sewage Disposal processing.
Experimental result is shown in Table 1.
1 logistics data table of table
Embodiment of the present invention has already been described in detail above, will be apparent to persons skilled in the art can do very much
Improvements and changes are without departing from essence spirit of the invention.All these changes and improvements all protection scope of the present invention it
It is interior.
Claims (10)
1. a kind of method of the processing containing sour ammonia-containing water, wherein the method comprises the following steps:
(1) after sour ammonia-containing water vacuum flashing will be contained, flashed vapour and lime set I are obtained；
(2) using lime set I obtained by step (1) using inert gas and/or natural gas as stripping medium in pretreater into
Promoting the circulation of qi mentions, and obtains sour gas I and lime set containing ammonia；
(3) it is sent after merging sour gas I obtained by flashed vapour obtained by step (1) and step (2) to sulfur recovery unit and is recycled；
(4) by the further air lift in ammonia still after exchanging heat of lime set containing ammonia obtained by step (2), sour gas II and lime set are obtained
II；By a part of gained lime set II after heat exchange heats up and generates gas-liquid two-phase, the ammonia still is recycled back to for containing to described
Ammonia lime set carries out air lift, and remaining lime set II is sent after exchanging heat to downstream units processing；
(5) sour gas II obtained by step (4) is carried out gas-liquid separation, obtains sour gas III and lime set III after heat exchange cooling；
Gained sour gas III is sent to sulfur recovery unit processing or is sent to the processing of torch pipe network；Gained lime set III is sent to downstream units
It is handled.
2. according to the method described in claim 1, wherein, in the step (1), the temperature of the vacuum flashing is 40-120
DEG C, preferably 55-75 DEG C, pressure 0.5-1.0MPaG, preferably 0.6-0.8MPaG；
Preferably, the vacuum flashing carries out in lime set flash tank, and the flashed vapour is obtained from the tank deck of the lime set flash tank
, the lime set I is obtained from the tank bottom of the lime set flash tank.
3. method according to claim 1 or 2, wherein in the step (2), the lime set I is sent to the pre- place
The tower top for managing tower makes the lime set I and the stripping medium counter current contacting in the tower of the pretreater carry out air lift；
Preferably, the condition of the air lift are as follows: 40-120 DEG C of operation temperature, preferably 55-75 DEG C, operating pressure 0.1-0.8MPaG,
It is preferred that 0.2-0.4MPaG；
Preferably, the inert gas is nitrogen；
Preferably, the natural gas is dry gas；
Preferably, the dosage of the stripping medium is 500-2000Nm3/ h, preferably 700-900Nm3/h；
Preferably, the sour gas I is obtained from the tower top of the pretreater；Tower of the lime set containing ammonia from the pretreater
Bottom obtain, and by the lime set containing ammonia sent after exchanging heat to, preferably by pump boosting after send to the tower top of the ammonia still into
Promoting the circulation of qi mentions.
4. method according to any one of claim 1-3, wherein be 100- in operation temperature in the step (4)
150 DEG C and operating pressure carry out the air lift under conditions of being 0.1-0.5MPaG；
Preferably, the lime set containing ammonia is divided into two parts, a part of lime set containing ammonia is through technique lime set heat exchanger and the lime set
II carries out indirect heat exchange, and another part lime set containing ammonia is through ammonia still process tower top cooler and the sour gas II, the preferably described acidity
The gaseous mixture of gas II and the high temperature flashed vapour from the external world carries out indirect heat exchange and then converges this two-part lime set containing ammonia
Lime set containing ammonia after being exchanged heat；
Preferably, the sour gas II is obtained from the tower top of the ammonia still.
5. method according to any of claims 1-4, wherein in the step (4), the lime set II is from described
The tower bottom of ammonia still obtains, it is preferable that uses temperature for 150-250 DEG C, preferably 150-180 DEG C a part of the lime set II
Low-pressure steam heat exchange, wherein the low-pressure steam is the saturation or overheat that pressure is 0.4-1.0MPaG, preferably 0.4-0.6MPaG
Steam；
Preferably, the low-pressure steam after heat exchanging carries out gas-liquid separation, with recovered steam lime set；It is further preferred that in steam
Gas-liquid separation is carried out to the low-pressure steam after the heat exchange in lime set water distributing can；
Preferably, the lime set II is warming up to 125-140 DEG C through heat exchange, to generate the gas-liquid two-phase；
Preferably, the gas-liquid two-phase is recycled back to the ammonia still and the counter current contacting of lime set containing ammonia carries out the air lift；
Preferably, the remaining lime set II is sent after exchanging heat and is used as shock chilling medium into coal gasification apparatus, or as complete
The recycle-water of factory, preferably as implement it is described processing the method containing sour ammonia-containing water device systems recycle-water.
6. method according to any one of claims 1-5, wherein in the step (5), the sour gas II is passed through
Ammonia still process tower top cooler and lime set containing ammonia are exchanged heat and are cooled down, preferably by the sour gas II and the high temperature flash distillation from the external world
It is exchanged heat and is cooled down with lime set containing ammonia through ammonia still process tower top cooler after gas mixing；
Preferably, temperature of the sour gas II after heat exchange cooling is 85-145 DEG C, preferably 100-135 DEG C, pressure 0.1-
0.3MPaG。
7. method according to claim 1 to 6, wherein right in gas-liquid separator in the step (5)
The sour gas II carries out gas-liquid separation；
Preferably, the sour gas III is obtained at the top of the gas-liquid separator；
Preferably, in the step (5), the sour gas III is the mixed gas that ammonia content is 10wt%-25wt%；
Preferably, the sour gas III is individually sent to sulfur recovery unit；
Preferably, the lime set III is sent to synthesis water treatment unit or thermoelectric device or is sent to Sewage Disposal
Reason.
8. it is a kind of for implementing the device systems of the method for the processing containing sour ammonia-containing water of any of claims 1-7,
Wherein, the device systems include:
Lime set flash tank；
Pretreater, the pretreater are connected to the downstream of the lime set flash tank in a manner of being in fluid communication；
Ammonia still, the ammonia still are connected to the downstream of the pretreater in a manner of being in fluid communication；
Ammonia still process tower top cooler, the ammonia still process tower top cooler are connected to the tower bottom of the pretreater in a manner of being in fluid communication
With the tower top of the ammonia still；
Gas-liquid separator, the gas-liquid separator are connected to the downstream of the ammonia still process tower top cooler in a manner of being in fluid communication；
Reboiler, the reboiler are connected to the tower bottom of the ammonia still in a manner of being in fluid communication；
Sulfur recovery unit, the sulfur recovery unit are connected to the lime set flash tank, the pretreatment in a manner of being in fluid communication
The downstream of tower and the gas-liquid separator；And
Technique lime set heat exchanger, the technique lime set heat exchanger be connected in a manner of being in fluid communication the ammonia still tower top and
The tower bottom of the pretreater.
9. device systems according to claim 8, wherein the pretreater has plate column or packed tower pattern；
Preferably, the packed tower pattern includes the packed tower pattern of random packing or structured packing；
Preferably, the pretreater has the packed tower pattern of random packing；
Preferably, the ammonia still has plate column or packed tower pattern；
Preferably, the packed tower pattern includes the packed tower pattern of random packing or structured packing；
Preferably, the ammonia still has the packed tower pattern of random packing.
10. device systems according to claim 8 or claim 9, wherein the device systems further include steam condensate and divide water
Tank, the steam condensate water distributing can are connected to the downstream of the reboiler in a manner of being in fluid communication；
Preferably, the device systems further include multiple pumps, and the multiple pump is separately positioned on the pretreater and institute
State between technique lime set heat exchanger and the ammonia still process tower top cooler, between the technique lime set heat exchanger and the ammonia still with
And the downstream of the gas-liquid separator.
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| CN112299664A (en) * | 2020-11-19 | 2021-02-02 | 赛鼎工程有限公司 | System and method for separating and recycling crushed coal pressure gasification gas water |
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