CN109704366A - A kind of technique and system of the coupling of pressurization deacidifion heat - Google Patents
A kind of technique and system of the coupling of pressurization deacidifion heat Download PDFInfo
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- CN109704366A CN109704366A CN201910109557.1A CN201910109557A CN109704366A CN 109704366 A CN109704366 A CN 109704366A CN 201910109557 A CN201910109557 A CN 201910109557A CN 109704366 A CN109704366 A CN 109704366A
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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
- C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors
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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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
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Abstract
The present invention relates to the techniques and system of a kind of pressurization deacidifion heat coupling, and the system comprises extracting tower, ammonia still, pump, condenser, heat exchanger, reboiler and valves；The top of the extracting tower is equipped with 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 and liquid phase return port, and bottom sets ammonium hydroxide outlet；Ammonia still process gas vent is set at the top of the ammonia still, top sets ammonia inlet and condensate inlet, and middle part sets alkali liquor inlet, and bottom sets liquid phase entrance and distilled ammonia wastewater outlet；The present invention is while guaranteeing that rich solution desorption pressures can be realized the recycling of substep desorption completion ammonolysis product, further increase ammonia still tower top pressure, ammonia still process column overhead temperatures are made to be higher than extracting tower column bottom temperature, heat with ammonia still process overhead condenser is extracting tower tower bottom heating, heat coupling is carried out by reasonable temperature schedule, to achieve energy-saving and emission reduction purposes.
Description
Technical field
The present invention relates to coke oven gas purification technical field more particularly to a kind of techniques of pressurization deacidifion heat coupling
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 constitutes the technique main body of absorption and desorption by wash mill and deacidifion device, and make the washing of ammonia and hydrogen sulfide and
Stripping desorption apparatus is closely linked.In absorptive unit, returned by deacidifion device containing the higher depickling lean solution of ammonia and
Water stripping absorbs the ammonia and hydrogen sulfide in raw coke oven gas, forms the rich solution containing ammonia and hydrogen sulfide, is vulcanized with reaching in removing raw coke oven gas
The purpose of hydrogen.In desorption unit, depickling lean solution and water stripping that rich solution is desorbed by deacidifion device be (distilled ammonia wastewater
A 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.Meanwhile rich solution desorbs
Process energy consumption is bigger than normal, operating cost is higher.Since tower bottom demand heat is big, generally use steam be passed directly into the mode of tower bottom into
Row heat supply, this also results in Waste water disadvantage bigger than normal.
The deacidifion of current mating ammonia spirit desulfurization process, for effectively recycling ammonolysis product and increase lean solution ratio of ammonia-sulfur can
Using the process of pressurization deacidifion.By improving rich solution desorption pressures, the recycling of ammonolysis product is completed in substep desorption
Meanwhile lean solution quality is improved, increase desulfurization effect.But the technique still has that energy consumption is high, operating cost is high, wastewater flow rate is inclined
Big problem.
Summary of the invention
The present invention provides the techniques and system of a kind of pressurization deacidifion heat coupling, are guaranteeing rich solution desorption pressures energy
While enough recycling for realizing substep desorption completion ammonolysis product, ammonia still tower top pressure is further increased, ammonia still process column overhead temperature is made
Degree is higher than extracting tower column bottom temperature, and the heat with ammonia still process overhead condenser is extracting tower tower bottom heating, passes through reasonable temperature system
Degree carries out heat coupling, to achieve energy-saving and emission reduction purposes.
In order to achieve the above object, the present invention is implemented with the following technical solutions:
A kind of technique of pressurization deacidifion heat coupling, includes the following steps:
1) by desulfurizing tower Lai rich solution mixed with remained ammonia, through heat exchanger and extracting tower lean solution heat exchange after enter extracting tower
Top；Ammonia evolution is inhibited by pressurized operation at the top of extracting tower, makes only to contain a small amount of ammonia in depickling column overhead acid gas product；
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) ammonia still top pressure is greater than extracting tower base pressure, and extracting tower tower bottom liquid phase is after pump pressurization, a part
Ammonia still process processing is carried out at the top of into ammonia still, the condenser that another part enters ammonia still process tower top is heated, the gas after heating
Liquid phase returns to depickling tower bottom；
4) ammonia still process gas evolution rear portion enters overhead condenser and carries out condensation concentration at the top of ammonia still, and in addition one
Part returns to depickling tower bottom as extracting tower bottom heat source by valve regulated；
5) for ammonia still process gas after condenser is concentrated, gas phase evolution becomes ammonolysis product at the top of ammonia still, and liquid phase returns to ammonia still
As reflux；
6) lye is added in the middle part of ammonia still and provides heat, ammonia still process by reboiler for removing fixed ammonia, ammonia still process tower bottom
Distilled ammonia wastewater a part of tower bottom discharge returns to desulfurization workshop section and is used as the water stripping that ammonia is washed in desulfurization, while to desulfurizing tower heat supply.
A kind of system of pressurization deacidifion heat coupling, including extracting tower, ammonia still, pump, condenser, heat exchanger, again
Boil device and valve；The top of the extracting tower is equipped with acid gas outlet, and top sets entry to mixed solution, and middle part sets lean solution side take-off
Mouthful, lower part sets ammonia still process gas access and liquid phase return port, and bottom sets ammonium hydroxide outlet；Wherein entry to mixed solution connects heat exchanger
The first heat transferring medium outlet, heat exchanger the first heat transferring medium entrance connection desulfurizing tower rich solution conveyance conduit and remained ammonia it is defeated
Send pipeline；The lean solution side line outlet of extracting tower is connect with the second heat transferring medium entrance of heat exchanger, and the second heat exchange of heat exchanger is situated between
Matter outlet connection lean solution conveyance conduit；Ammonia still process gas vent is set at the top of the ammonia still, top sets ammonia inlet and condensate liquid
Entrance, middle part set alkali liquor inlet, and bottom sets liquid phase entrance and distilled ammonia wastewater outlet；The ammonium hydroxide outlet and pump of the extracting tower
Entrance connection, the outlet of pump is separately connected the ammonia inlet of ammonia still and the first heat transferring medium entrance of condenser, condenser
The first heat transferring medium outlet connection extracting tower liquid phase return port；The ammonia still process gas vent of ammonia still by pipeline all the way with
Second heat transferring medium entrance of condenser connects, and the ammonia still process gas access of extracting tower, and and ammonia still process are connected by another way pipeline
Valve is set on the pipeline of gas access connection；The second heat transferring medium outlet connection ammonia product pipeline of condenser, condenser
The condensate inlet of condensate outlet connection ammonia still；The distilled ammonia wastewater outlet of ammonia still is connect with distilled ammonia wastewater pipeline, ammonia still process
Waste pipe is connected by the entrance of lateral and reboiler, and the outlet of reboiler and the liquid phase entrance of ammonia still connect,
In addition the distilled ammonia wastewater pipeline in lateral downstream connects water stripping conveyance conduit.
The extracting tower is between entry to mixed solution and lean solution side take-off mouth, lean solution side take-off mouth and ammonia still process gas
Multiple filling layers or tower tray is respectively set in 2 sections of tower bodies between body entrance.
The ammonia still is in 2 sections between ammonia inlet and alkali liquor inlet, between alkali liquor inlet and liquid phase entrance
Multiple filling layers or tower tray are respectively set in tower body.
Compared with prior art, the beneficial effects of the present invention are:
1) by improving ammonia still tower top pressure, so that ammonia still process column overhead temperatures are higher than extracting tower column bottom temperature, in ammonia still process
While tower condenser completes concentration ammonia, heat supply also is carried out to desulfurizing tower as the reboiler of desulfurizing tower；
2) in such a way that heat couples, System steam consumption, while area needed for making ammonia still tower bottom reboiler are reduced
It reduces；By the way of steam indirect heating, wastewater displacement is reduced.
Detailed description of the invention
Fig. 1 is the flow chart of the technique of pressurization deacidifion heat coupling of the present invention.
In figure: 1. extracting tower, 11. acid gas outlet, 12. entry to mixed solution, 13. lean solution side take-off mouth, 14. ammonia still process gas
21. ammonia still process gas vent of body entrance 15. liquid phase return port, one 16. ammonium hydroxide outlet, 2. ammonia still, 22. ammonia inlet
23. 24. alkali liquor inlet of condensate inlet, 25. liquid phase entrance, 26. distilled ammonia wastewater exports 3. heat exchangers 4. pump, 5. condensation
6. reboiler of device, 7. valve
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 technique of pressurization deacidifion heat coupling of the present invention, includes the following steps:
1) by desulfurizing tower Lai rich solution mixed with remained ammonia, through heat exchanger 3 and extracting tower lean solution heat exchange after enter depickling
1 top of tower；Ammonia evolution is inhibited by pressurized operation at the top of extracting tower 1, is made in 1 tower top acid gas product of extracting tower only containing a small amount of
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) 2 top pressure of ammonia still is greater than 1 base pressure of extracting tower, and 1 tower bottom liquid phase of extracting tower is after 4 pressurization of pump, and one
Part, which enters, carries out ammonia still process processing at the top of ammonia still 2, the condenser 5 that another part enters the top of ammonia still 2 is heated, and is heated
Liquid phase afterwards returns to 1 bottom of extracting tower；
4) 2 top ammonia still process gas of ammonia still evolution rear portion enters overhead condenser 5 and carries out condensation concentration, in addition
A part is adjusted by valve 7 returns to 1 bottom of extracting tower as 1 bottom heat source of extracting tower；
5) for 2 top ammonia still process gas of ammonia still after the concentration of condenser 5, gas phase evolution becomes ammonolysis product, and liquid phase returns to ammonia still process
Tower 2 is as reflux；
6) lye is added in the middle part of ammonia still 2 and provides heat by reboiler 6 for removing fixed ammonia, 2 bottom of ammonia still, steams
Distilled ammonia wastewater a part of 2 bottom of ammonia tower discharge returns to desulfurization workshop section and is used as the water stripping that ammonia is washed in desulfurization, while supplying desulfurizing tower
Heat.
A kind of system of pressurization deacidifion heat coupling, including extracting tower 1, ammonia still 2, pump 4, condenser 5, heat exchanger
3, reboiler 6 and valve 7；The top of the extracting tower 1 is equipped with acid gas outlet 11, and top sets entry to mixed solution 12, and middle part is set
Lean solution side take-off mouth 13, lower part set ammonia still process gas access 14 and liquid phase return port 15, and bottom sets ammonium hydroxide outlet 16；Wherein
Entry to mixed solution 12 connects the first heat transferring medium outlet of heat exchanger 3, and the first heat transferring medium entrance of heat exchanger 3 connects desulfurizing tower
Rich solution conveyance conduit and remained ammonia conveyance conduit；The lean solution side line outlet 13 of extracting tower 1 and the second heat transferring medium of heat exchanger 3
Entrance connection, the second heat transferring medium outlet connection lean solution conveyance conduit of heat exchanger 3；The top of the ammonia still 2 sets ammonia still process gas
Body outlet 21, top sets ammonia inlet 22 and condensate inlet 23, and middle part sets alkali liquor inlet 24, bottom set liquid phase entrance 25 and
Distilled ammonia wastewater outlet 26；The ammonium hydroxide outlet 16 of the extracting tower 1 is connected with the entrance of pump 4, and the outlet for pumping 4 is separately connected ammonia still process
The ammonia inlet 22 of tower 2 and the first heat transferring medium entrance of condenser 5, the first heat transferring medium outlet connection depickling of condenser 5
The liquid phase return port 15 of tower 1；The ammonia still process gas vent 21 of ammonia still 2 is situated between by the second heat exchange of pipeline all the way and condenser 5
The connection of matter entrance, the ammonia still process gas access 14 of extracting tower 1 is connected by another way pipeline, and connect with ammonia still process gas access 14
Valve 7 is set on pipeline；The second heat transferring medium outlet connection ammonia product pipeline of condenser 5, the condensate outlet of condenser 5 connect
Connect the condensate inlet 23 of ammonia still 2；The distilled ammonia wastewater outlet 26 of ammonia still 2 is connect with distilled ammonia wastewater pipeline, distilled ammonia wastewater pipe
Road is connect by lateral with the entrance of reboiler 6, and the outlet of reboiler 6 is connect with the liquid phase entrance 25 of ammonia still 2, point
In addition the distilled ammonia wastewater pipeline in branch pipe(tube) downstream connects water stripping conveyance conduit.
The extracting tower 1 is between entry to mixed solution 12 and lean solution side take-off mouth 13, lean solution side take-off mouth 13
Multiple filling layers or tower tray is respectively set in 2 sections of tower bodies between ammonia still process gas access 14.
The ammonia still 2 is between ammonia inlet 22 and alkali liquor inlet 24, alkali liquor inlet 24 and liquid phase entrance 25
Between 2 sections of tower bodies in multiple filling layers or tower tray is respectively set.
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 technique of pressurization deacidifion heat coupling, which comprises the steps of:
1) by desulfurizing tower Lai rich solution mixed with remained ammonia, through heat exchanger and extracting tower lean solution heat exchange after enter extracting tower top
Portion；Ammonia evolution is inhibited by pressurized operation at the top of extracting tower, makes 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) ammonia still top pressure is greater than extracting tower base pressure, and after pump pressurization, a part enters extracting tower tower bottom liquid phase
Ammonia still process processing is carried out at the top of ammonia still, the condenser that another part enters ammonia still process tower top is heated, the liquid phase after heating
Return to depickling tower bottom；
4) ammonia still process gas evolution rear portion enters overhead condenser and carries out condensation concentration, another part at the top of ammonia still
Depickling tower bottom is returned as extracting tower bottom heat source by valve regulated；
5) for ammonia still process gas after condenser is concentrated, gas phase evolution becomes ammonolysis product at the top of ammonia still, and liquid phase returns to ammonia still conduct
Reflux；
6) lye is added in the middle part of ammonia still and provides heat, ammonia still bottom by reboiler for removing fixed ammonia, ammonia still process tower bottom
Distilled ammonia wastewater a part of portion's discharge returns to desulfurization workshop section and is used as the water stripping that ammonia is washed in desulfurization, while to desulfurizing tower heat supply.
2. it is a kind of pressurization deacidifion heat coupling system, which is characterized in that including extracting tower, ammonia still, pump, condenser,
Heat exchanger, reboiler and valve；The top of the extracting tower is equipped with acid gas outlet, and top sets entry to mixed solution, and middle part sets poor
Liquid side take-off mouth, lower part set ammonia still process gas access and liquid phase return port, and bottom sets ammonium hydroxide outlet；Wherein entry to mixed solution
Connect heat exchanger the first heat transferring medium outlet, heat exchanger the first heat transferring medium entrance connection desulfurizing tower rich solution conveyance conduit and
Remained ammonia conveyance conduit；The lean solution side line outlet of extracting tower is connect with the second heat transferring medium entrance of heat exchanger, heat exchanger
Second heat transferring medium outlet connection lean solution conveyance conduit；Ammonia still process gas vent is set at the top of the ammonia still, top sets ammonium hydroxide and enters
Mouth and condensate inlet, middle part set alkali liquor inlet, and bottom sets liquid phase entrance and distilled ammonia wastewater outlet；The ammonium hydroxide of the extracting tower
Outlet is connected with the entrance of pump, and the first heat transferring medium of ammonia inlet and condenser that the outlet of pump is separately connected ammonia still enters
Mouthful, the liquid phase return port of the first heat transferring medium outlet connection extracting tower of condenser；The ammonia still process gas vent of ammonia still passes through
The second heat transferring medium entrance of pipeline and condenser connects all the way, is entered by the ammonia still process gas that another way pipeline connects extracting tower
Mouthful, and valve is set on the pipeline connecting with ammonia still process gas access；The second heat transferring medium outlet connection ammonia product pipe of condenser
Road, the condensate inlet of the condensate outlet connection ammonia still of condenser；Distilled ammonia wastewater outlet and the distilled ammonia wastewater pipe of ammonia still
Road connection, distilled ammonia wastewater pipeline are connected by the entrance of lateral and reboiler, the outlet of reboiler and the gas-liquid of ammonia still
In addition the connection of phase entrance, the distilled ammonia wastewater pipeline in lateral downstream connect water stripping conveyance conduit.
3. a kind of system of pressurization deacidifion heat coupling according to claim 2, which is characterized in that the extracting tower
In 2 sections of towers between entry to mixed solution and lean solution side take-off mouth, between lean solution side take-off mouth and ammonia still process gas access
Multiple filling layers or tower tray are respectively set in vivo.
4. a kind of system of pressurization deacidifion heat coupling according to claim 2, which is characterized in that the ammonia still
Multilayer is respectively set in 2 sections of tower bodies between ammonia inlet and alkali liquor inlet, between alkali liquor inlet and liquid phase entrance
Filler or tower tray.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910109557.1A CN109704366B (en) | 2019-02-11 | 2019-02-11 | Pressurized deacidification ammonia distillation heat coupling process and system |
| PCT/CN2020/070522 WO2020164341A1 (en) | 2019-02-11 | 2020-01-06 | Process and system for thermal coupling of pressurized deacidification and ammonia distillation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910109557.1A CN109704366B (en) | 2019-02-11 | 2019-02-11 | Pressurized deacidification ammonia distillation heat coupling process and system |
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| Publication Number | Publication Date |
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| CN109704366A true CN109704366A (en) | 2019-05-03 |
| CN109704366B CN109704366B (en) | 2023-08-01 |
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ID=66264225
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| CN201910109557.1A Active CN109704366B (en) | 2019-02-11 | 2019-02-11 | Pressurized deacidification ammonia distillation heat coupling process and system |
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| CN (1) | CN109704366B (en) |
| WO (1) | WO2020164341A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN113150837A (en) * | 2021-04-23 | 2021-07-23 | 济南冶金化工设备有限公司 | Coke oven gas desulfurization process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114200981B (en) * | 2021-11-04 | 2023-06-02 | 金盛海洋科技股份有限公司 | System and method for controlling temperature of top of distillation column |
| CN115367943B (en) * | 2022-08-22 | 2024-02-02 | 吴嘉 | Energy-saving salt-containing heavy ammonia nitrogen-containing wastewater treatment system and process |
| CN117069346B (en) * | 2023-10-16 | 2024-02-02 | 天津市创举科技股份有限公司 | Residual ammonia water distillation benzene removal device and application method thereof |
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| 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 |
| CN113150837A (en) * | 2021-04-23 | 2021-07-23 | 济南冶金化工设备有限公司 | Coke oven gas desulfurization process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109704366B (en) | 2023-08-01 |
| WO2020164341A1 (en) | 2020-08-20 |
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