CN106673014A - Process of removing sulfur and ammonia from coke gas to prepare ammonia water - Google Patents
Process of removing sulfur and ammonia from coke gas to prepare ammonia water Download PDFInfo
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- CN106673014A CN106673014A CN201611249990.8A CN201611249990A CN106673014A CN 106673014 A CN106673014 A CN 106673014A CN 201611249990 A CN201611249990 A CN 201611249990A CN 106673014 A CN106673014 A CN 106673014A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/12—Separation of ammonia from gases and vapours
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/16—Hydrogen sulfides
- C01B17/167—Separation
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/022—Preparation of aqueous ammonia solutions, i.e. ammonia water
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
- C10K1/122—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors containing only carbonates, bicarbonates, hydroxides or oxides of alkali-metals (including Mg)
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- Engineering & Computer Science (AREA)
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Abstract
The invention discloses a process of removing sulfur and ammonia from coke gas to prepare ammonia water. On the basis of existing AS methods, ammonia in the coke gas serves as an alkali source, ammonia water containing solution serves as a medium, the ammonia and hydrogen sulfide in the coke gas are removed by cyclic ammonia/sulfur absorption, desulphurizing, ammonia-washing rich solution pressurization, deabsorption and regeneration process, and meanwhile the remaining ammonia water is processed by a low-pressure ammonia distilling tower which takes remaining heat of a system as a heat source, and 5-20% of ammonia water is byproduct in the process. The process comprises an ammonia and hydrogen sulfide absorption part, an ammonia and hydrogen deabsorption part and remaining ammonia water based ammonia distilling part. Clean gas produced by the process can meet requirements of Admittance Standard of Coking Industry, and the process disclosed by the invention has the advantages of short process flow, low operation cost, good resource utilization and good environmental protection effect.
Description
Technical field
The invention belongs to chemical technology field, specifically a kind of coke oven gas desulfurization Study of Deamination is for ammonia technique.
Background technology
At present, domestic coke oven gas desulfurization deamination mainly have ammonia sulfur cycle washing method (i.e. AS methods) with ammonia as alkali source and with
Ammonia is the wet oxidation process (i.e. HPF methods) of alkali source, and list of references is：Luan Zhen space .AS methods wash ammonia sulfur removal technology with operation [J]. river
Northern chemical industry, 2010,33 (5)：59-60；Wang Jianhua, analysis and the improvement [J] of Li Shuai .AS method coal gas desulfurization techniques. fuel and change
Work, 2008,39 (4)：49-50；The application of Cui little Jun, Li Guang .HPF method sulfur removal technologies and improvement [J]. fuel and chemical industry, 2007,
38(3)：53-55；Dong Yanjun, Xu Daoliang, Zheng Xianyong. the improvement of coke-stove gas HPF method sulfur removal technologies and application [J]. Guangzhou
Work, 2013,41 (8)：183-184.Production practices show that both techniques all there are problems that many.AS method coal gas desulfurizations, net ammonia
Effect poor (reason is that deacidifion effect is poor, and amount of liquor is little), general coal gas desulfurization washes sulfide hydrogen about 400- after ammonia
600mg/Nm3, containing ammonia about 100mg/Nm3, index request is not reached, production management has high demands plant running (five tower through transports), ammonia is provided
Source (burning) is without utilization.HPF methods have that desulfurization waste liquor is difficult, sulfur purity is low, regenerator tail gas ammon amount is high, pollution is empty
The problems such as gas, while HPF methods adopt the inferior chemical fertilizer-ammonium sulfate of valuable gas washing in SA production, without economic benefit.Therefore, open
The coke oven gas desulfurization Study of Deamination that to send out a kind of new is imperative for ammonia technique.
The content of the invention
For the deficiencies in the prior art, the technical problem that the present invention is intended to solve is to provide a kind of coke oven gas desulfurization deamination
Prepare ammonia technique.On the basis of existing AS methods, with the ammonia in coke-stove gas as alkali source, water containing ammonia is Jie to the technique
Matter, the ammonia washed in ammonia rich solution pressing and desorption regeneration technology removing coke-stove gas using ammonia sulfur cycle absorption, desulfurization and hydrogen sulfide, together
Shi Liyong system waste heats process remained ammonia, the ammonia of by-product 5~20% in technique as the low pressure ammonia still of thermal source.Technique stream
Journey includes the desorption part and the remained ammonia ammonia still process part that absorb part, ammonia and hydrogen sulfide of ammonia and hydrogen sulfide.The technique productions
Purified gas can reach the requirement of " coking industry permit standard ", technological process is short, operating cost is low, the utilization of resources good, environmental protection
It is profitable.
The present invention solves the technical scheme of the technical problem and is to provide a kind of coke oven gas desulfurization Study of Deamination for ammonia work
Skill, it is characterised in that the technique is comprised the following steps：
(1) the absorption part of ammonia and hydrogen sulfide：Absorption tower is disposed with from the bottom up desulfurization section, washes ammonia section and alkali cleaning
Section；Temperature is 22~25 DEG C, ammonia content is 6~8g/Nm3, hydrogen sulfide content be 6~8g/Nm3Coke-stove gas be introduced into absorption
The desulfurization section of tower bottom, with the deacidification lean solution for washing the rich ammonia of ammonia section all or part out and desorber middle part side take-off
Counter current contacting, removes the hydrogen sulfide in coke-stove gas；Coke-stove gas after removing hydrogen sulfide washes ammonia in the middle part of absorption tower
Section, the whole waste water counter current contactings with low pressure ammonia still tower reactor remove the ammonia in coal gas；When low pressure ammonia still tower reactor whole waste water
Amount it is inadequate when, supplement the waste water of desorber tower reactor, remove the ammonia in coal gas；Topmost on absorption tower is provided with alkali wash section,
Using remaining trace hydrogen sulfide in alkali liquor absorption coke-stove gas, the alkali liquor after the completion of washing is divided into two parts and is sent to low pressure respectively
The bottom of ammonia still and the bottom of desorber, decompose solid ammonium-salt therein；On alkali wash section top, demister is set；Due to washing
Ammonia, ammonia desulfurization are exothermic reaction, are to keep desulfurization to wash the low-temperature operation of ammonia overall process, absorption tower desulfurization section and wash ammonia
Section is provided with cooler, so that the ammonia content in the coke-stove gas after absorption tower is processed reaches 30mg/Nm3, hydrogen sulfide content
Reach 200mg/Nm3；The rich ammonia in part described in the absorption part of ammonia and hydrogen sulfide is the 1/3-1/2 of all richness ammonia quality；
(2) desorption part of ammonia and hydrogen sulfide：By step 1) in absorb the rich solution of hydrogen sulfide and ammonia and be pressurized with pump, supercharging
After be divided into two parts, a part is the cold rich solution for accounting for total mass flow rate 20~25%, another part for account for total mass flow rate 75~
80% hot rich solution, is then sent to respectively desorber；Not preheated cold rich solution is directly entered into desorber top, to absorb solution
Inhale the ammonia in the sour gas of column overhead；Hot rich solution is lean with the deacidification of desorbing tower bottoms, desorber middle part side take-off respectively
Liquid is exchanged heat to 105~115 DEG C, and subsequently into desorber middle and upper part, desorber bottom sets reboiler heating, and thermal source is low pressure steaming
Vapour, the gauge pressure of steam is not less than 1.0MPa；Sour gas in rich solution is escaped from desorbing column overhead, is sent to next workshop section；Desorbing
Tower mixed gas of the middle part lateral line withdrawal function containing ammonia, are divided into gas-liquid two-phase after dephlegmator, then complete gas through flash tank
The separation of liquid mixture, gas phase enter back into condensate cooler cooling, strong aqua ammonia can be obtained, from dephlegmator lime set out as return
Flow liquid is sent to desorber or low pressure ammonia still；Meanwhile, one deacidification lean solution of side take-off is sent absorption tower back to and is taken off in the middle part of desorber
Sulfur section is recycled as absorbing liquid；The waste water of desorber tower reactor in addition to part is used as to wash ammonia and is sent to absorption tower and washes ammonia section,
Remaining goes biochemical treatment；Desorber is operated under the pressure that gauge pressure is 0.5~0.6MPa, and desorbing column overhead temperatures are 50~65
DEG C, the hydrogen sulfide content in deacidification lean solution maintains below 100ppm, and the hydrogen sulfide content in desorbing tower bottoms maintains 50ppm
Hereinafter, ammonia content maintains below 150ppm；
(3) remained ammonia ammonia still process part：Coke oven gas desulfurization Study of Deamination is for residual coking ammonia water in ammonia technique using low
Pressure ammonia still process, desorber middle part side take-off ammonia through dephlegmator lime set or absorption tower wash ammonia section part out
Rich ammonia is also directed to the process of low pressure ammonia still；The mixed liquor Jing feed coolers for accounting for total mass flow rate 20~25% are cooled to into 35
~40 DEG C enter low pressure ammonia still top, and remaining mixed liquor exchanges heat to 85~95 DEG C with low pressure ammonia still process tower bottoms and steamed into low pressure
Ammonia tower middle and upper part, low pressure ammonia still adopts reboiler indirect heating manner, and most of thermal source is the waste water or solution of desorber tower reactor
The deacidification lean solution of tower middle part side take-off is inhaled, its waste heat source is low-pressure steam；The sour gas of low pressure ammonia still overhead extraction, send
Toward next workshop section；Mixed gas of the low pressure ammonia still middle and upper part side take-off containing ammonia, successively into ammonia dephlegmator and condensation cooling
Device is cooled down, and strong aqua ammonia can be obtained, and low pressure ammonia still is sent to as backflow from ammonia dephlegmator lime set out；Low pressure ammonia still tower
The deacidifion waste water of kettle first goes to be preheated to mixed liquor, and afterwards again Jing gaseous effluent coolers cooling whole is sent to absorption tower and washes ammonia section；
Low pressure ammonia still is operated under the pressure of 0.05~0.1MPa of gauge pressure, and tower top temperature is 55~65 DEG C, the sulfuration in tower reactor waste water
Hydrogen content maintains below 50ppm, and ammonia content maintains below 150ppm；Part richness ammonia in remained ammonia ammonia still process part
Water is the 1/2-2/3 of all richness ammonia quality.
Step 1) described in alkali liquor be sodium hydroxide solution that concentration is 5%~40%.Step 2) in cold rich solution temperature be
23~27 DEG C.
Compared with prior art, beneficial effect of the present invention is：
(1) absorption tower alkali wash section is arranged on and washes ammonia section top, and reason is from washing hydrogen sulfide in the coal gas out of ammonia section top
Content is higher, is conducive to washing ammonia process.In order to prevent entrainment, demister is increased above alkali wash section.
(2) desorber adopts pressurized operation, can increase the relative volatility of ammonia and hydrogen sulfide, makes the sour gas of tower top
In the ammonia amount taken out of be greatly decreased；The ammonia concn of the deacidification lean solution of desulfurization section is sent in increase, increases substantially ratio of ammonia-sulfur, improves
Desulfuration efficiency；The temperature for making desorber tower reactor is raised, and then the ammonium salt in its liquid phase is decomposed as far as possible, and to gas phase transfer.
(3) ammonia in coke-stove gas is substantially all from desorber middle part side take-off, and ammonia concentration is higher, can make dense
Ammonia, while the dense ammonia of low pressure ammonia still middle and upper part extraction also can strong aqua ammonia processed.This strong aqua ammonia can be sent to desulphurization denitration workshop section
Or take out, the by-product value in whole technical process can be improved.
(4) residual coking ammonia water enters low pressure ammonia still ammonia still process, and tower reactor is using reboiler indirect heating manner, part of heat energy
The waste water of desorber tower reactor or the deacidification lean solution of middle part side take-off, with desorber economic benefits and social benefits pattern is formed, and fully saves energy consumption；Its
Waste heat source is low-pressure steam.
(5) desorber and low pressure ammonia still are all to use steam indirectly heat by reboiler, different from AS sulfur removal technologies
Direct steam heating, while reaching effect, reduce a large amount of discharge of wastewater, not only reduced environmental protection pressure but also saved steam
Consumption, it is with the obvious advantage.
In sum, the present invention with ammonia as alkali source, water containing ammonia as medium, using ammonia sulfur cycle absorb, regeneration removing
The technique of ammonia and hydrogen sulfide in coke-stove gas reaches not only can ammonia and hydrogen sulfide content behind absorption tower in coke-stove gas
The discharge standard of the national requirements of " coking industry permit standard "；Take off while certain density strong aqua ammonia being obtained and being sent to desulfurization
Nitre workshop section or take-away, improve the by-product value in whole technical process；Wastewater discharge can be finally greatly decreased, environmental protection pressure is bright
It is aobvious to reduce.Again the worry without doctor solution salt extraction, the net ammonia of regeneration tail gas, belongs to Environmentally-sound technology.
Description of the drawings
Fig. 1 is integrated artistic flow chart of the coke oven gas desulfurization Study of Deamination of the present invention for a kind of embodiment of ammonia technique；
Specific embodiment
The specific embodiment of the present invention is given below.Specific embodiment is only used for further describing the present invention, does not limit
The application scope of the claims processed.
The invention provides a kind of coke oven gas desulfurization Study of Deamination is for ammonia technique (referring to Fig. 1), it is characterised in that the work
Skill is comprised the following steps：
(1) the absorption part of ammonia and hydrogen sulfide：Absorbing the capital equipment of part has absorption tower and supporting heat exchanger, storage
Tank etc..Absorption tower from the bottom up by desulfurization section, wash ammonia section and alkali wash section is constituted.Temperature is 22~25 DEG C, ammonia content is 6~8g/
Nm3, hydrogen sulfide content be 6~8g/Nm3Coke-stove gas be introduced into the desulfurization section of absorption tower bottom, wash ammonia section with absorption tower middle part
All or part of richness ammonia (ammonia density is 0.35~0.7%) out and the deacidification lean solution of desorber middle part side take-off
(ammonia density is 1.7~2.9%) counter current contacting, by ammonia and hydrogen sulfide chemical reaction is carried out in absorption tower, reaches removing burnt
The purpose of the hydrogen sulfide in producer gas；Coke-stove gas after removing hydrogen sulfide washes ammonia section in the middle part of absorption tower, with low pressure
Whole waste water (below ammonia density 100ppm) of ammonia still tower reactor and desorber tower reactor effluent part (ammonia density 150ppm with
Under) counter current contacting, the ammonia in the larger principle removing coal gas of the dissolubility using ammonia in water；Ammonia in order to ensure coal gas contains
Amount touches the mark, and can increase waste water circulation amount, but in order to reduce the thermic load of the reboiler of desorber, washes the richness after ammonia
Used as desulfurization section absorbing liquid, another part is sent to the regeneration of low pressure ammonia still to an ammonia part.Topmost on absorption tower is provided with
Alkali wash section, adopts concentration for 20~30% alkali liquor (NaOH solution) and absorbs remaining trace hydrogen sulfide in coke-stove gas, washing
After the completion of alkali liquor be divided into two parts and be sent to the bottom of desorber and the bottom of low pressure ammonia still respectively, decompose Stagnant ammonium therein
Salt.In order to reduce the entrainment of alkali liquor, demister is set on alkali wash section top.Exothermic reaction is due to washing ammonia, ammonia desulfurization,
To keep desulfurization to wash the low-temperature operation of ammonia overall process, absorption tower desulfurization section and wash ammonia section and be provided with cooler, so as to inhale
The ammonia content received in the coke-stove gas after tower reaches 30mg/Nm3, hydrogen sulfide content reach 200mg/Nm3.The suction of ammonia and hydrogen sulfide
The rich ammonia in part described in receiving portions is the 1/3-1/2 of all richness ammonia quality；
(2) desorption part of ammonia and hydrogen sulfide：The capital equipment of desorption part has desorber and supporting heat exchanger, storage
Tank etc..By step 1) in absorb the rich solution of hydrogen sulfide and ammonia and be pressurized with pump, be divided into two parts after supercharging, a part is to account for total matter
The cold rich solution (23~27 DEG C) of amount flow 20~25%, another part is the hot rich solution for accounting for total mass flow rate 75~80%, then
Desorber is sent to respectively；Not preheated cold rich solution is directly entered into desorber top by tower top, with absorption and desorption column overhead
Ammonia in sour gas；Hot rich solution is exchanged heat respectively with the deacidification lean solution of desorbing tower bottoms, desorber middle part side take-off
To 105~115 DEG C, subsequently into desorber middle and upper part, desorber bottom sets reboiler heating, and thermal source is low-pressure steam, steam
Gauge pressure is not less than 1.0MPa；The sour gas (concentration is more than 96%) of desorber overhead extraction sulfide hydrogen, carbon dioxide, send
Toward next workshop section.Desorber middle part lateral line withdrawal function is divided into gas containing the mixed gas that ammonia density is 9~16% after dephlegmator
Liquid is biphase, and the separation of gas-liquid mixture is then completed through flash tank, and gas phase enters back into condensate cooler cooling, concentration can be obtained
For 5~20% strong aqua ammonia (as side-product), it is sent to desorber as backflow from dephlegmator lime set out or low pressure is steamed
Ammonia tower.Meanwhile, one ammonia content of side take-off is that 1.7~2.9% deacidification lean solution sends absorption tower desulfurization back in the middle part of desorber
Duan Zuowei absorbing liquids are recycled.The waste water of desorber tower reactor is higher due to saliferous, and major part removes biochemistry, and remainder is used as washing
Ammonia is sent to absorption tower and washes ammonia section.Desorber is operated under the pressure that gauge pressure is 0.5~0.6MPa, and desorbing column overhead temperatures are 50
~65 DEG C, the hydrogen sulfide content in deacidification lean solution maintains below 100ppm, and the hydrogen sulfide content in desorbing tower bottoms is maintained
Below 50ppm, ammonia content maintains below 150ppm.In desorber, decompose the alkali liquor (NaOH solution) needed for solid ammonium-salt,
Alkali wash section in absorption tower.
(3) remained ammonia ammonia still process part：The capital equipment of remained ammonia ammonia still process part has low pressure ammonia still and with buing or get by illegal means
Hot device, storage tank etc..Coke oven gas desulfurization Study of Deamination is for residual coking ammonia water in ammonia technique using the process of low pressure ammonia still, desorbing
Tower middle part side take-off ammonia through dephlegmator lime set or absorption tower wash ammonia section out part richness ammonia be also directed to low pressure
Ammonia still process；The mixed liquor Jing feed coolers for accounting for total mass flow rate 20~25% are cooled to into 35~40 DEG C to steam into low pressure
Ammonia top of tower, remaining mixed liquor exchanges heat to 85~95 DEG C with low pressure ammonia still process tower bottoms and enters low pressure ammonia still middle and upper part, low pressure
Ammonia still adopts reboiler indirect heating manner, most of thermal source to be the waste water of desorber tower reactor or the deacidification of middle part side take-off
Lean solution, with desorber economic benefits and social benefits pattern is formed, and fully saves energy consumption, and its waste heat source is the low-pressure steam that gauge pressure is 0.5MPa.Low pressure
The sour gas (concentration is more than 85%) of ammonia still overhead extraction sulfide hydrogen, carbon dioxide, is sent to next workshop section.Low pressure is steamed
Ammonia tower middle and upper part side take-off is successively cold into ammonia dephlegmator and condensate cooler containing the mixed gas that ammonia density is 5%~7%
But, the strong aqua ammonia (as side-product) that concentration is 5~20% can be obtained, be sent to as backflow from ammonia dephlegmator lime set out
Low pressure ammonia still.The deacidifion waste water of low pressure ammonia still tower reactor first goes pre- to mixed liquor because temperature is high and salinity is less
Heat, afterwards again Jing gaseous effluent coolers cooling whole is sent to absorption tower and washes ammonia section.Low pressure ammonia still is 0.05~0.1MPa in gauge pressure
Pressure under operate, tower top temperature be 55~65 DEG C, the hydrogen sulfide content in tower reactor waste water maintains below 50ppm, ammonia content
Maintain below 150ppm.In low pressure ammonia still, decompose the alkali liquor (NaOH solution) needed for solid ammonium-salt, in absorption tower
Alkali wash section.Part richness ammonia in remained ammonia ammonia still process part is the 1/2-2/3 of all richness ammonia quality.
The present invention does not address part and is applied to prior art.
Claims (3)
1. a kind of coke oven gas desulfurization Study of Deamination is for ammonia technique, it is characterised in that the technique is comprised the following steps：
（1）The absorption part of ammonia and hydrogen sulfide：Absorption tower is disposed with from the bottom up desulfurization section, washes ammonia section and alkali wash section；Temperature
It is 6 ~ 8g/Nm to spend for 22 ~ 25 DEG C, ammonia content3, hydrogen sulfide content be 6 ~ 8g/Nm3Coke-stove gas be introduced into absorption tower bottom
Desulfurization section, connects with the deacidification lean solution adverse current for washing the rich ammonia of ammonia section all or part out and desorber middle part side take-off
Touch, remove the hydrogen sulfide in coke-stove gas；Coke-stove gas after removing hydrogen sulfide washes ammonia section in the middle part of absorption tower, and low
Whole waste water counter current contactings of pressure ammonia still tower reactor, remove the ammonia in coal gas；When low pressure ammonia still tower reactor whole waste water amount not
When enough, the waste water of desorber tower reactor is supplemented, remove the ammonia in coal gas；Topmost on absorption tower is provided with alkali wash section, using alkali
Liquid absorbs remaining trace hydrogen sulfide in coke-stove gas, and the alkali liquor after the completion of washing is divided into two parts and is sent to low pressure ammonia still respectively
Bottom and desorber bottom, decompose solid ammonium-salt therein；On alkali wash section top, demister is set；Due to washing ammonia, ammonia
Water desulfurization is exothermic reaction, is to keep desulfurization to wash the low-temperature operation of ammonia overall process, absorption tower desulfurization section and wash ammonia Duan Jun
Cooler is provided with, so that the ammonia content in the coke-stove gas after absorption tower is processed reaches 30mg/Nm3, hydrogen sulfide content reaches
200mg/Nm3；The rich ammonia in part described in the absorption part of ammonia and hydrogen sulfide is the 1/3-1/2 of all richness ammonia quality；
（2）The desorption part of ammonia and hydrogen sulfide：By step 1）In absorb the rich solution of hydrogen sulfide and ammonia and be pressurized with pump, after supercharging point
For two parts, a part is the cold rich solution for accounting for total mass flow rate 20 ~ 25%, and another part is the heat for accounting for total mass flow rate 75 ~ 80%
Rich solution, is then sent to respectively desorber；Not preheated cold rich solution is directly entered into desorber top, with absorption and desorption column overhead
Sour gas in ammonia；Hot rich solution is changed respectively with the deacidification lean solution of desorbing tower bottoms, desorber middle part side take-off
To 105 ~ 115 DEG C, subsequently into desorber middle and upper part, desorber bottom sets reboiler heating to heat, and thermal source is low-pressure steam, steam
Gauge pressure is not less than 1.0MPa；Sour gas in rich solution is escaped from desorbing column overhead, is sent to next workshop section；Desorber middle part side line
Extract the mixed gas containing ammonia out, gas-liquid two-phase is divided into after dephlegmator, then complete gas-liquid mixture through flash tank
Separate, gas phase enters back into condensate cooler cooling, and strong aqua ammonia can be obtained, and solution is sent to as backflow from dephlegmator lime set out
Inhale tower or low pressure ammonia still；Meanwhile, one deacidification lean solution of side take-off sends absorption tower desulfurization section back to as suction in the middle part of desorber
Receive liquid to recycle；In addition to part is used as to wash ammonia and is sent to absorption tower and washes ammonia section, remaining goes life to the waste water of desorber tower reactor
Change is processed；Desorber is operated in the case where gauge pressure is for the pressure of 0.5 ~ 0.6MPa, and desorbing column overhead temperatures are 50 ~ 65 DEG C, deacidification lean solution
In hydrogen sulfide content maintain below 100ppm, the hydrogen sulfide content in desorbing tower bottoms maintains below 50ppm, ammonia content
Maintain below 150ppm；
（3）Remained ammonia ammonia still process part：Coke oven gas desulfurization Study of Deamination is steamed for residual coking ammonia water in ammonia technique using low pressure
Ammonia tower process, desorber middle part side take-off ammonia through dephlegmator lime set or absorption tower wash ammonia section out part richness ammonia
Water is also directed to the process of low pressure ammonia still；The mixed liquor Jing feed coolers for accounting for total mass flow rate 20 ~ 25% are cooled to into 35 ~ 40 DEG C
Into low pressure ammonia still top, remaining mixed liquor exchanges heat to 85 ~ 95 DEG C with low pressure ammonia still process tower bottoms and enters in low pressure ammonia still
Top, low pressure ammonia still adopts reboiler indirect heating manner, and most of thermal source is in the waste water or desorber of desorber tower reactor
The deacidification lean solution of portion's side take-off, its waste heat source is low-pressure steam；The sour gas of low pressure ammonia still overhead extraction, is sent to next
Workshop section；Mixed gas of the low pressure ammonia still middle and upper part side take-off containing ammonia, successively cool down into ammonia dephlegmator and condensate cooler,
Strong aqua ammonia can be obtained, low pressure ammonia still is sent to as backflow from ammonia dephlegmator lime set out；Low pressure ammonia still tower reactor it is de-
Sour distilled ammonia wastewater first goes to be preheated to mixed liquor, and afterwards again Jing gaseous effluent coolers cooling whole is sent to absorption tower and washes ammonia section；Low pressure is steamed
Ammonia tower is operated under the pressure of 0.05 ~ 0.1MPa of gauge pressure, and tower top temperature is 55 ~ 65 DEG C, the hydrogen sulfide content dimension in tower reactor waste water
Hold in below 50ppm, ammonia content maintains below 150ppm；Part richness ammonia in remained ammonia ammonia still process part is for all
The 1/2-2/3 of rich ammonia quality.
2. coke oven gas desulfurization Study of Deamination according to claim 1 is for ammonia technique, it is characterised in that step 1）Described in
Alkali liquor is the sodium hydroxide solution that concentration is 5% ~ 40%.
3. coke oven gas desulfurization Study of Deamination according to claim 1 is for ammonia technique, it is characterised in that step 2）In cold richness
Liquid temp is 23 ~ 27 DEG C.
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107777708A (en) * | 2017-09-28 | 2018-03-09 | 华陆工程科技有限责任公司 | A kind of method of thick ammonia refining in acidic water stripping device |
| CN107880947A (en) * | 2017-12-15 | 2018-04-06 | 中冶焦耐(大连)工程技术有限公司 | A kind of multifunctional combined scrubbing tower and coal gas combine washing methods |
| CN108793090A (en) * | 2018-09-17 | 2018-11-13 | 陕西黑猫焦化股份有限公司 | The method and apparatus of preparing sulfuric acid from hydrogen sulfide in a kind of abjection coal gas |
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| CN110523230A (en) * | 2019-09-27 | 2019-12-03 | 中冶焦耐(大连)工程技术有限公司 | A kind of energy-efficient deacidifion technique and system |
| CN111087004A (en) * | 2019-12-23 | 2020-05-01 | 首钢水城钢铁（集团）有限责任公司 | Method for treating residual ammonia water in coal gasification production and recovery of coke oven |
| CN111655825A (en) * | 2018-03-14 | 2020-09-11 | 三菱重工工程株式会社 | Gas refining device |
| CN113896265A (en) * | 2021-11-02 | 2022-01-07 | 天津市创举科技股份有限公司 | Ammonia distillation treatment process for residual ammonia water |
| CN114229939A (en) * | 2021-12-27 | 2022-03-25 | 中冶焦耐(大连)工程技术有限公司 | High-efficiency energy-saving ammonia distillation process |
| CN114604829A (en) * | 2022-03-21 | 2022-06-10 | 中国能源建设集团广东省电力设计研究院有限公司 | System and method for purifying hydrogen from coke oven gas |
| CN114836246A (en) * | 2022-04-04 | 2022-08-02 | 上海圣升化工科技有限公司 | Process for purifying and recycling coke oven gas to recover high-quality concentrated ammonia water and sulfur |
| CN115612531A (en) * | 2022-12-16 | 2023-01-17 | 天津市创举科技股份有限公司 | Process and equipment for recovering ammonia from coke oven gas |
| CN116216830A (en) * | 2023-01-28 | 2023-06-06 | 中冶焦耐(大连)工程技术有限公司 | Energy-saving deacidification ammonia distillation process and device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107777708A (en) * | 2017-09-28 | 2018-03-09 | 华陆工程科技有限责任公司 | A kind of method of thick ammonia refining in acidic water stripping device |
| CN107880947A (en) * | 2017-12-15 | 2018-04-06 | 中冶焦耐(大连)工程技术有限公司 | A kind of multifunctional combined scrubbing tower and coal gas combine washing methods |
| CN111655825A (en) * | 2018-03-14 | 2020-09-11 | 三菱重工工程株式会社 | Gas refining device |
| CN111655825B (en) * | 2018-03-14 | 2021-06-22 | 三菱重工工程株式会社 | Gas refining device |
| CN108793090A (en) * | 2018-09-17 | 2018-11-13 | 陕西黑猫焦化股份有限公司 | The method and apparatus of preparing sulfuric acid from hydrogen sulfide in a kind of abjection coal gas |
| 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 |
| WO2020164341A1 (en) * | 2019-02-11 | 2020-08-20 | 中冶焦耐(大连)工程技术有限公司 | Process and system for thermal coupling of pressurized deacidification and ammonia distillation |
| CN110523230A (en) * | 2019-09-27 | 2019-12-03 | 中冶焦耐(大连)工程技术有限公司 | A kind of energy-efficient deacidifion technique and system |
| CN111087004A (en) * | 2019-12-23 | 2020-05-01 | 首钢水城钢铁（集团）有限责任公司 | Method for treating residual ammonia water in coal gasification production and recovery of coke oven |
| CN113896265A (en) * | 2021-11-02 | 2022-01-07 | 天津市创举科技股份有限公司 | Ammonia distillation treatment process for residual ammonia water |
| CN114229939A (en) * | 2021-12-27 | 2022-03-25 | 中冶焦耐(大连)工程技术有限公司 | High-efficiency energy-saving ammonia distillation process |
| CN114229939B (en) * | 2021-12-27 | 2024-04-26 | 中冶焦耐(大连)工程技术有限公司 | Efficient energy-saving ammonia distillation process |
| CN114604829A (en) * | 2022-03-21 | 2022-06-10 | 中国能源建设集团广东省电力设计研究院有限公司 | System and method for purifying hydrogen from coke oven gas |
| CN114836246A (en) * | 2022-04-04 | 2022-08-02 | 上海圣升化工科技有限公司 | Process for purifying and recycling coke oven gas to recover high-quality concentrated ammonia water and sulfur |
| CN114836246B (en) * | 2022-04-04 | 2023-09-19 | 上海圣升化工科技有限公司 | Process for purifying coke oven gas and recycling high-quality strong ammonia water and sulfur |
| CN115612531A (en) * | 2022-12-16 | 2023-01-17 | 天津市创举科技股份有限公司 | Process and equipment for recovering ammonia from coke oven gas |
| CN116216830A (en) * | 2023-01-28 | 2023-06-06 | 中冶焦耐(大连)工程技术有限公司 | Energy-saving deacidification ammonia distillation process and device |
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