CN109647150A - A kind of pressurization deacidifion technique and system - Google Patents
A kind of pressurization deacidifion technique and system Download PDFInfo
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- CN109647150A CN109647150A CN201910109566.0A CN201910109566A CN109647150A CN 109647150 A CN109647150 A CN 109647150A CN 201910109566 A CN201910109566 A CN 201910109566A CN 109647150 A CN109647150 A CN 109647150A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
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Abstract
The present invention relates to a kind of pressurization deacidifion technique and systems, by desulfurizing tower Lai rich solution mixed with remained ammonia, enter extracting tower top after the heat exchange of the lean solution of heat exchanger and extracting tower, ammonia evolution is inhibited by pressurized operation at the top of extracting tower, extracting tower tower bottom liquid phase carries out ammonia still process processing after pump pressurization, into ammonia still top；Ammonia still top gas phase escapes rear portion and returns to depickling tower bottom, and another part enters overhead condenser and carries out concentration；Gas phase evolution after condenser is concentrated becomes ammonolysis product, and liquid phase returns to ammonia still as reflux；Lye is added in the middle part of ammonia still for removing fixed ammonia, bottom is passed through steam as tower bottom heat source；Distilled ammonia wastewater is discharged in ammonia still process tower bottom, and part returns to desulfurization workshop section and is used as the water stripping that ammonia is washed in desulfurization.The present invention improves lean solution quality by changing rich solution desorption pressures while the recycling of ammonolysis product is completed in substep desorption, increases desulfurization effect.
Description
Technical field
The present invention relates to coke oven gas purification technical field more particularly to a kind of pressurization deacidifion techniques and system.
Background technique
Ammonia spirit desulfurization technique is a kind of for removing the common technology of hydrogen sulfide in raw coke oven gas.The technique is in coal gas
Ammonia is alkali source, using water containing ammonia as washing medium, combines the hydrogen sulfide in washing (absorption) technique removing coal gas using ammonia sulphur.
The method is made of the technique main body of absorption and desorption wash mill and deacidifion device, and makes washing and the vapour of ammonia and hydrogen sulfide
Desorption apparatus is mentioned to be closely linked.In absorptive unit, is returned by deacidifion device and contain the higher depickling lean solution of ammonia and vapour
Water lift absorbs the ammonia and hydrogen sulfide in raw coke oven gas, forms the rich solution containing ammonia and hydrogen sulfide, to reach hydrogen sulfide in removing raw coke oven gas
Purpose.In desorption unit, depickling lean solution and water stripping (the one of distilled ammonia wastewater that rich solution is desorbed by deacidifion device
Part) send wash mill recycling back to.
Ammonia desulfurizing process is only the absorption of alkali source by ammonia in washing medium, coal gas of water compared to other sulfur removal technologies
Method desulfurization, does not generate desulfurization waste liquor, has the advantages that overall gas purification process is short, investment is low.But it is desorbed in prior art
Unit (deacidifion) desorbs ammonia and hydrogen sulfide together, and the gas desorbed carries out sulfur recovery after ammonolysis craft.This process
In, the ammonia that can be used as chemical end-products is treated as impurity and directly decomposes, and fails effectively to be recycled.
The deacidifion of current mating ammonia spirit desulfurization process, due in sulfur removing pregnant solution hydrogen sulfide and ammonia one be sent to a place under guard
It inhales, it is difficult to the individually desorption quantity of control hydrogen sulfide and ammonia.When deacidifion tower tower bottom stripping duty increases, it can increase in lean solution
The escaped quantity of ammonia causes lean solution insufficient containing ammonia, is difficult to meet desulfurization requirement when returning to desulfurizing tower.If deacidifion tower tower bottom vapour
Load reduction is proposed, and will lead to hydrogen sulfide cannot effectively be extracted from rich solution, causes hydrogen sulfide from tower top escaped quantity
While insufficient, lean solution contains that hydrogen sulfide is more, is equally difficult to meet the desulfurization requirement in desulfurizing tower.
Summary of the invention
The present invention provides a kind of pressurization deacidifion technique and systems, and by changing rich solution desorption pressures, substep is desorbed
While completing the recycling of ammonolysis product, lean solution quality is improved, increases desulfurization effect.
In order to achieve the above object, the present invention is implemented with the following technical solutions:
A kind of pressurization deacidifion technique, includes the following steps:
1) by desulfurizing tower Lai rich solution mixed with remained ammonia, through the lean solution of heat exchanger and extracting tower heat exchange after enter depickling
Tower top, extracting tower top inhibit ammonia evolution by pressurized operation, make only to contain a small amount of ammonia in depickling column overhead acid gas product
Gas；
2) by escaping at the top of extracting tower, the lean solution and desulfurizing tower rich solution and remained ammonia of extracting tower side take-off exchange heat acid gas
Afterwards, desulfurizing tower is returned to be recycled；
3) extracting tower tower bottom liquid phase carries out ammonia still process processing into ammonia still top after pump pressurization；
4) ammonia still top gas phase evolution rear portion return depickling tower bottom, another part enter overhead condenser into
Row concentration；
5) the gas phase evolution after condenser is concentrated becomes ammonolysis product, and liquid phase returns to ammonia still as reflux；
6) lye is added in the middle part of ammonia still for removing fixed ammonia, bottom is passed through steam as tower bottom heat source；Ammonia still bottom
Distilled ammonia wastewater is discharged in portion, and part returns to desulfurization workshop section and is used as the water stripping that ammonia is washed in desulfurization.
The tower top operating pressure of the extracting tower is 0.2~0.8MPaG.
A kind of pressurization deacidifion system, including extracting tower, ammonia still, heat exchanger, condenser and pump；The extracting tower
Top sets acid gas outlet, and top sets entry to mixed solution, and middle part sets lean solution side take-off mouth, and lower part sets ammonia still process gas access, bottom
If ammonium hydroxide outlet；First heat exchange of the first heat transferring medium of the entry to mixed solution and heat exchanger outlet connection, heat exchanger is situated between
Matter entrance is separately connected residual ammonia water pipeline and desulfurizing tower rich solution pipeline；The the second heat transferring medium entrance and lean solution side line of heat exchanger
Produce mouth connection, the second heat transferring medium outlet connection lean solution output channel；Ammonia still process gas vent is set at the top of ammonia still, top is set
Ammonia inlet and phegma entrance, middle part set alkali liquor inlet, and lower part sets steam inlet, and bottom sets distilled ammonia wastewater outlet；Extracting tower
Ammonium hydroxide outlet by pump connection ammonia still ammonia inlet；The ammonia still process gas vent of ammonia still is separately connected the steaming of extracting tower
Ammonia gas entrance and condenser inlet, the phegma entrance of the condensate outlet connection ammonia still of condenser, the gas phase of condenser
Outlet connection ammonia conveyance conduit；The distilled ammonia wastewater outlet of ammonia still is separately connected distilled ammonia wastewater conveyance conduit and water stripping conveying
Pipeline.
Setting multiple filling layers or tower tray, the lean solution in extracting tower between the entry to mixed solution and lean solution side take-off mouth
Setting multiple filling layers or tower tray in extracting tower between side take-off mouth and ammonia still process gas access.
Compared with prior art, the beneficial effects of the present invention are:
1) by changing rich solution desorption pressures, substep is desorbed, effectively recycling ammonolysis product, is increased economic efficiency；
2) desulfurization lean solution quality is improved, desulfurization effect is reinforced.
Detailed description of the invention
Fig. 1 is a kind of flow chart for deacidifion technique of pressurizeing of the present invention.
In figure: 1. extracting tower, 11. acid gas exports 12. entry to mixed solution, 13. lean solution side take-off mouth, 14. ammonia still process gas
23. phegma entrance of entrance 15. ammonium hydroxide outlet, 2. ammonia still, 21. ammonia still process gas vent, 22. ammonia inlet, 24. lye
25. steam inlet of entrance, 26. distilled ammonia wastewater outlet, 3. pump 4. condenser, 5. heat exchanger
Specific embodiment
Specific embodiments of the present invention will be further explained with reference to the accompanying drawing:
As shown in Figure 1, a kind of pressurization deacidifion technique, includes the following steps:
1) by desulfurizing tower Lai rich solution mixed with remained ammonia, enter after the heat exchange of the lean solution of heat exchanger 5 and extracting tower 1 de-
1 top of acid tower inhibits ammonia evolution by pressurized operation at the top of extracting tower 1, makes in 1 tower top acid gas product of extracting tower only containing few
Measure ammonia；
2) by escaping at the top of extracting tower 1, lean solution and the desulfurizing tower rich solution and remained ammonia of 1 side take-off of extracting tower change acid gas
After heat, returns to desulfurizing tower and be recycled；
3) 1 tower bottom liquid phase of extracting tower by pump 3 pressurization after, into ammonia still 2 at the top of carry out ammonia still process processing；
4) 2 top gas phase of ammonia still evolution rear portion returns to 1 bottom of extracting tower, and another part enters overhead condenser
4 carry out concentration；
5) the gas phase evolution after the concentration of condenser 4 becomes ammonolysis product, and liquid phase returns to ammonia still 2 as reflux；
6) lye is added in the middle part of ammonia still 2 for removing fixed ammonia, bottom is passed through steam as tower bottom heat source；Ammonia still 2
Distilled ammonia wastewater is discharged in bottom, and part returns to desulfurization workshop section and is used as the water stripping that ammonia is washed in desulfurization.
The tower top operating pressure of the extracting tower 1 is 0.2~0.8MPaG.
A kind of pressurization deacidifion system, including extracting tower 1, ammonia still 2, heat exchanger 5, condenser 4 and pump 3；It is described de-
The top of acid tower 1 sets acid gas outlet 11, and top sets entry to mixed solution 12, and middle part sets lean solution side take-off mouth 13, and lower part sets ammonia still process
Gas access 14, bottom set ammonium hydroxide outlet 15；First heat transferring medium of the entry to mixed solution 12 and heat exchanger 5, which exports, to be connected
It connects, the first heat transferring medium entrance of heat exchanger 5 is separately connected residual ammonia water pipeline and desulfurizing tower rich solution pipeline；The of heat exchanger 5
Two heat transferring medium entrances are connect with lean solution side take-off mouth 13, the second heat transferring medium outlet connection lean solution output channel；Ammonia still 2
Top set ammonia still process gas vent 21, top sets ammonia inlet 22 and phegma entrance 23, and middle part sets alkali liquor inlet 24, and lower part is set
Steam inlet 25, bottom set distilled ammonia wastewater outlet 26；The ammonium hydroxide that the ammonium hydroxide outlet 15 of extracting tower 1 passes through 3 connection ammonia still 2 of pump
Entrance 22；The ammonia still process gas vent 21 of ammonia still 2 is separately connected 4 entrance of ammonia still process gas access 14 and condenser of extracting tower 1, cold
The phegma entrance 23 of the condensate outlet connection ammonia still 2 of condenser 4, the gaseous phase outlet of condenser 4 connect ammonia conveyance conduit；
The distilled ammonia wastewater outlet 26 of ammonia still 2 is separately connected distilled ammonia wastewater conveyance conduit and water stripping conveyance conduit.
Setting multiple filling layers or tower tray, institute in extracting tower 1 between the entry to mixed solution 12 and lean solution side take-off mouth 13
State setting multiple filling layers or tower tray in the extracting tower 1 between lean solution side take-off mouth 13 and ammonia still process gas access 14.
The foregoing is only a preferred embodiment of the present invention, but scope of protection of the present invention is not limited thereto,
Anyone skilled in the art in the technical scope disclosed by the present invention, according to the technique and scheme of the present invention and its
Inventive concept is subject to equivalent substitution or change, should be covered by the protection scope of the present invention.
Claims (4)
1. a kind of pressurization deacidifion technique, which comprises the steps of:
1) by desulfurizing tower Lai rich solution mixed with remained ammonia, through the lean solution of heat exchanger and extracting tower heat exchange after enter extracting tower on
Portion, extracting tower top inhibit ammonia evolution by pressurized operation, make only to contain a small amount of ammonia in depickling column overhead acid gas product；
2) acid gas at the top of extracting tower by escaping, after lean solution and desulfurizing tower rich solution and the remained ammonia heat exchange of extracting tower side take-off,
Desulfurizing tower is returned to be recycled；
3) extracting tower tower bottom liquid phase carries out ammonia still process processing into ammonia still top after pump pressurization；
4) ammonia still top gas phase evolution rear portion returns to depickling tower bottom, and it is dense that another part enters overhead condenser progress
Contracting processing；
5) the gas phase evolution after condenser is concentrated becomes ammonolysis product, and liquid phase returns to ammonia still as reflux；
6) lye is added in the middle part of ammonia still for removing fixed ammonia, bottom is passed through steam as tower bottom heat source；Ammonia still process tower bottom row
Distilled ammonia wastewater out, part return to desulfurization workshop section and are used as the water stripping that ammonia is washed in desulfurization.
2. pressurization deacidifion technique according to claim 1, which is characterized in that the tower top operating pressure of the extracting tower
For 0.2~0.8MPaG.
3. a kind of pressurization deacidifion system, which is characterized in that including extracting tower, ammonia still, heat exchanger, condenser and pump；Institute
It states and sets acid gas outlet at the top of extracting tower, top sets entry to mixed solution, and middle part sets lean solution side take-off mouth, and lower part sets ammonia still process gas
Entrance, bottom set ammonium hydroxide outlet；First heat transferring medium of the entry to mixed solution and heat exchanger outlet connection, the of heat exchanger
One heat transferring medium entrance is separately connected residual ammonia water pipeline and desulfurizing tower rich solution pipeline；Second heat transferring medium entrance of heat exchanger with
The connection of lean solution side take-off mouth, the second heat transferring medium outlet connection lean solution output channel；Ammonia still process gas is set at the top of ammonia still to go out
Mouthful, top sets ammonia inlet and phegma entrance, and middle part sets alkali liquor inlet, and lower part sets steam inlet, and bottom sets distilled ammonia wastewater and goes out
Mouthful；The ammonia inlet that the ammonium hydroxide outlet of extracting tower passes through pump connection ammonia still；The ammonia still process gas vent of ammonia still is separately connected
The ammonia still process gas access of extracting tower and condenser inlet, the phegma entrance of the condensate outlet connection ammonia still of condenser are cold
The gaseous phase outlet of condenser connects ammonia conveyance conduit；Ammonia still distilled ammonia wastewater outlet be separately connected distilled ammonia wastewater conveyance conduit and
Water stripping conveyance conduit.
4. a kind of pressurization deacidifion system according to claim 3, which is characterized in that the entry to mixed solution and lean solution
Setting multiple filling layers or tower tray in extracting tower between side take-off mouth, between the lean solution side take-off mouth and ammonia still process gas access
Setting multiple filling layers or tower tray in extracting tower.
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| CN201910109566.0A CN109647150A (en) | 2019-02-11 | 2019-02-11 | A kind of pressurization deacidifion technique and system |
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| CN201910109566.0A CN109647150A (en) | 2019-02-11 | 2019-02-11 | A kind of pressurization deacidifion technique and system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
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|---|---|---|---|---|
| CN105984886A (en) * | 2015-02-05 | 2016-10-05 | 薛斌 | Process for producing anhydrous ammonia by ammonia distillation and deacidification |
| CN105985814A (en) * | 2015-02-09 | 2016-10-05 | 上海同特化工科技有限公司 | Treatment technology for removing hydrogen sulfide, hydrogen cyanide and ammonia in coal gas |
| 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 |
| CN209771782U (en) * | 2019-02-11 | 2019-12-13 | 中冶焦耐(大连)工程技术有限公司 | Pressurization deacidification ammonia distillation system |
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2019
- 2019-02-11 CN CN201910109566.0A patent/CN109647150A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105984886A (en) * | 2015-02-05 | 2016-10-05 | 薛斌 | Process for producing anhydrous ammonia by ammonia distillation and deacidification |
| CN105985814A (en) * | 2015-02-09 | 2016-10-05 | 上海同特化工科技有限公司 | Treatment technology for removing hydrogen sulfide, hydrogen cyanide and ammonia in coal gas |
| 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 |
| CN209771782U (en) * | 2019-02-11 | 2019-12-13 | 中冶焦耐(大连)工程技术有限公司 | Pressurization deacidification ammonia distillation system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
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