CN220467588U - Change condensate ammonia resource recovery unit - Google Patents
Change condensate ammonia resource recovery unit Download PDFInfo
- Publication number
- CN220467588U CN220467588U CN202321990685.XU CN202321990685U CN220467588U CN 220467588 U CN220467588 U CN 220467588U CN 202321990685 U CN202321990685 U CN 202321990685U CN 220467588 U CN220467588 U CN 220467588U
- Authority
- CN
- China
- Prior art keywords
- stage
- dephlegmator
- ammonia
- acid gas
- stripping tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 83
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 40
- 238000011084 recovery Methods 0.000 title claims description 4
- 239000002253 acid Substances 0.000 claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 44
- 239000002994 raw material Substances 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 21
- 238000005406 washing Methods 0.000 claims description 18
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 7
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 40
- 238000004064 recycling Methods 0.000 abstract description 5
- 239000003245 coal Substances 0.000 abstract description 4
- 239000003250 coal slurry Substances 0.000 abstract description 4
- 238000002360 preparation method Methods 0.000 abstract description 4
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 3
- 230000007797 corrosion Effects 0.000 abstract description 3
- 238000005260 corrosion Methods 0.000 abstract description 3
- 238000000354 decomposition reaction Methods 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 abstract description 3
- 230000007547 defect Effects 0.000 abstract 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 6
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000008213 purified water Substances 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The utility model relates to a device for recycling ammonia resources of a conversion condensate, which aims to solve the problems that the original technology has the defects that condensate enters a coal slurry preparation working section, the environment of a coal mill room is bad, ammonia nitrogen is accumulated in a system to cause system corrosion, ammonia resources are wasted, a large amount of ammonia is entrained in an acid gas sent to a torch, the decomposition temperature of the ammonia is high, and the ammonia cannot be decomposed at the temperature of the acid gas torch, so that the environment protection is generated.
Description
Technical Field
The utility model belongs to the field of chemical production, and particularly relates to a device for recycling ammonia resources of a conversion condensate.
Background
The stripping system of the CO conversion unit of the coal chemical industry device is mainly used for treating low-temperature process condensate of the CO conversion unit and ammonia washing liquid of the acid gas removal unit, stripping ammonia, hydrogen sulfide, carbon dioxide and other gases in the condensate and ammonia washing liquid, recycling purified condensate into the gasification device, separating gas from liquid after condensing the stripped ammonia gas, delivering the acid gas (CO 2 and H2S) to a torch for burning, and removing the separated condensate into a coal slurry preparation section.
The prior art has the following problems: (1) the condensate enters a coal slurry preparation working section, so that the coal mill room has a bad environment, ammonia nitrogen is accumulated in the system, and a series of problems such as system corrosion and waste of ammonia resources are caused; (2) acid gas (CO 2 and H2S) is sent to a torch to be entrained with a large amount of ammonia, the decomposition temperature of the ammonia is high, and the ammonia cannot be decomposed at the temperature of the acid gas torch, so that the problem of environmental protection is generated.
Disclosure of Invention
In order to solve the problems that the original process has condensate entering a coal slurry preparation section, so that the coal mill room has severe environment, ammonia nitrogen is accumulated in a system to cause system corrosion, ammonia resources are wasted, a large amount of ammonia is carried in an acid gas sent to a torch, the decomposition temperature of the ammonia is high, and the ammonia cannot be decomposed at the temperature of the acid gas torch, thereby generating environmental protection.
The utility model designs a device for recycling ammonia resources of a conversion condensate, which comprises a raw material water tank, a stripping tower b, a feeding cooler, an acid gas separator, a first-stage preheater, a second-stage preheater, a first-stage dephlegmator, a second-stage dephlegmator and a third-stage dephlegmator, wherein the second-stage condenser, the third-stage condenser, the dephlegmator, an acid gas heater and a washing liquid cooler;
the raw material water tank is provided with a raw material water pump which is divided into two paths, one path is connected with the upper part of the stripping tower b through a feeding cooler, and the other path is connected with the upper middle part of the stripping tower b through a primary preheater and a secondary preheater in sequence;
the top of the stripping tower b is connected with an acid gas separator, the middle of the stripping tower b is connected with a first-stage preheater, the first-stage preheater is connected with the middle of a first-stage dephlegmator, the top of the first-stage dephlegmator is connected with the middle of a second-stage dephlegmator through a second-stage condenser, the top of the second-stage dephlegmator is connected with the middle of a third-stage dephlegmator through a third-stage condenser, the bottom of the first-stage dephlegmator and the bottom of the second-stage dephlegmator are connected with the middle of a raw material water tank together through a connecting dephlegmator and a third-stage dephlegmator, and the top of the third-stage dephlegmator discharges gas;
the bottom of the acid gas separator is connected with the middle part of the raw material water tank, and the top of the acid gas separator discharges gas through an acid gas heater;
the bottom of the stripping tower b is provided with a purification water pump b, the stripping tower b is divided into two paths after being connected with a secondary preheater through the purification water pump b, one path is directly discharged, and the other path is sequentially connected with an acid gas heater and a washing liquid cooler to the top of the stripping tower b.
And steam is directly introduced into the bottom of the stripping tower b and is used as a heat source of a heating medium.
One part of raw water entering the raw water tank is dilute ammonia water generated by condensation of an original stripping system, and the other part is conversion condensate and ammonia washing liquid.
The utility model has the advantages that:
the technology adopts the process routes of raw material water combined distribution, single-tower pressurized steam stripping, side stream extraction and three-stage fractional condensation, upgrades and reforms the original conversion condensate steam stripping system, recovers ammonia resources of the original conversion steam stripping system, produces pure ammonia gas products, can be directly used for desulfurization and denitrification of boilers, solves the environmental protection problem, and generates good economic benefit.
Drawings
FIG. 1 is a schematic diagram of a raw stripping system and feed water combination;
FIG. 2 is a schematic illustration of the present utility model;
reference numerals illustrate: 1. an ammonia washing tower; 2. a stripping tower a; 3. a preheater; 4. an exhaust gas cooler; 5. a gas-liquid separator; 6. a purifying water pump a; 7. a raw material water tank; 8. a raw material water pump; 9. a stripping column b; 10. a feed cooler; 11. an acid gas separator; 12. a purifying water pump b; 13. a secondary preheater; 14. a primary preheater; 15. a first-stage dephlegmator; 16. a second-stage condenser; 17. a secondary dephlegmator; 18. a three-stage condenser; 19. a three-stage dephlegmator; 20. a partial condensate cooler; 21. an acid gas heater; 22. a washing liquid cooler; 5-1, dilute ammonia water; 1-1, condensate liquid conversion and ammonia liquor washing.
Detailed Description
As shown in fig. 1:
after the raw materials are treated by the stripping system, the raw materials to be treated are divided into two parts, wherein one part is dilute ammonia water 5-1 generated by condensation of the original stripping system, and the other part is conversion condensate and ammonia washing liquid 1-1.
The utility model relates to a device for recycling ammonia resources of a conversion condensate, which is shown in fig. 2, and comprises a raw material water tank 7, a stripping tower b9, a feed cooler 10, an acid gas separator 11, a primary preheater 14, a secondary preheater 13, a primary dephlegmator 15, a secondary dephlegmator 17, a tertiary dephlegmator 19, a secondary condenser 16, a tertiary condenser 18, a dephlegmator 20, an acid gas heater 21 and a washing liquid cooler 22;
the raw material water tank 7 is provided with a raw material water pump 8 which is divided into two paths, one path is connected with the upper part of the stripping tower b9 through a feeding cooler 10, and the other path is connected with the upper middle part of the stripping tower b9 through a primary preheater 14 and a secondary preheater 13 in sequence;
the top of the stripping tower b9 is connected with an acid gas separator 11, the middle of the stripping tower b9 is connected with a first-stage preheater 14, the first-stage preheater 14 is connected with the middle of a first-stage dephlegmator 15, the top of the first-stage dephlegmator 15 is connected with the middle of a second-stage dephlegmator 17 through a second-stage condenser 16, the top of the second-stage dephlegmator 17 is connected with the middle of a third-stage dephlegmator 19 through a third-stage condenser 18, the bottom of the first-stage dephlegmator 15 and the bottom of the second-stage dephlegmator 17 are connected with the bottom of the third-stage dephlegmator 19 through a connecting dephlegmator 20 together to be connected with the middle of a raw material water tank 7, and the top of the third-stage dephlegmator 19 discharges gas;
the bottom of the acid gas separator 11 is connected with the middle part of the raw material water tank 7, and the top of the acid gas separator 11 discharges gas through an acid gas heater 21;
the bottom of the stripping tower b9 is provided with a purification water pump b12, the stripping tower b9 is divided into two paths after being connected with the secondary preheater 13 through the purification water pump b12, one path is directly discharged, and the other path is sequentially connected with the acid gas heater 21 and the washing liquid cooler 22 to the top of the stripping tower b 9.
Steam is directly introduced into the bottom of the stripping tower b9 and is used as a heat source of a heating medium.
One part of raw water entering the raw water tank 7 is dilute ammonia water 5-1 generated by condensation in an original stripping system, and the other part is conversion condensate and ammonia washing liquid 1-1.
The working process of the utility model comprises the following steps: the dilute ammonia water 5-1 produced by condensation from an original stripping system is mixed with a conversion condensate and ammonia washing liquid 1-1 in a raw material water tank 7 and then is pressurized by a raw material water pump 8 to be divided into two paths, one path is taken as cold feed, is cooled by a feed cooler 10 and then enters the upper part of a stripping tower b9, the other path is taken as hot feed, firstly carries out primary heat exchange with side line gas through a primary preheater 14, then carries out secondary heat exchange with tower bottom liquid through a secondary preheater 13, then enters the middle-upper part of the stripping tower b9 for stripping, and the stripping tower 9 directly enters the bottom of the stripping tower b9 by taking low-pressure steam as a heat source.
Free ammonia, carbon dioxide and hydrogen sulfide are transferred from the liquid phase to steam, and most of the ammonia, carbon dioxide and hydrogen sulfide enter the gas phase when reaching the upper section of the stripping tower b 9; the cold feed absorbs ammonia and water vapor in the gas phase, in order to further reduce the ammonia content in the acid gas, a stream of purified water is introduced from the top of the tower, cooled by a washing liquid cooler 22, enters the top of a stripping tower b9, and when the purified water is discharged from the top of the stripping tower b9 as washing water, the main components of the acid gas are carbon dioxide and hydrogen sulfide, and are discharged from the top of the stripping tower b9, then the purified water enters an acid gas separator 11 for gas-liquid separation, the separated liquid phase returns to a raw material water tank 7, and the acid gas is heated by an acid gas heater 21 and is discharged into an acid gas torch or a sulfur recovery device.
In the ammonia enrichment area in the middle of the stripping tower b9, ammonia-containing steam is extracted from the side line of the stripping tower b9, the ammonia-containing steam extracted from the side line is cooled step by step through a first-stage condenser 14, a second-stage condenser 16 and a third-stage condenser 18 respectively, then gas-liquid separation is carried out in the first-stage condenser 15, the second-stage condenser 17 and the third-stage condenser 19, after the liquid phase separated in the second-stage is cooled by a condensate separating cooler 20, the liquid phase is mixed with the liquid phase separated in the third-stage, and then the mixture returns to the raw material water tank 7 again, and pure ammonia separated from the third-stage condenser 19 is led out of the device.
The technology adopts the process routes of raw material water combined distribution, single-tower pressurized steam stripping, side stream extraction and three-stage fractional condensation, upgrades and reforms the original conversion condensate steam stripping system, recovers ammonia resources of the original conversion steam stripping system, produces pure ammonia gas products, can be directly used for desulfurization and denitrification of boilers, solves the environmental protection problem, and generates good economic benefit.
Claims (3)
1. The utility model provides a transform condensate ammonia resource recovery unit, includes raw materials water pitcher (7), stripper b (9), its characterized in that: the device also comprises a feed cooler (10), an acid gas separator (11), a first-stage preheater (14), a second-stage preheater (13), a first-stage dephlegmator (15), a second-stage dephlegmator (17), a third-stage dephlegmator (19), a second-stage condenser (16), a third-stage condenser (18), a dephlegmator cooler (20), an acid gas heater (21) and a washing liquid cooler (22);
the raw material water tank (7) is provided with a raw material water pump (8) which is divided into two paths, one path is connected with the upper part of the stripping tower b (9) through a feeding cooler (10), and the other path is connected with the upper middle part of the stripping tower b (9) through a primary preheater (14) and a secondary preheater (13) in sequence;
the top of the stripping tower b (9) is connected with an acid gas separator (11), the middle of the stripping tower b (9) is connected with a first-stage preheater (14), the first-stage preheater (14) is connected with the middle of a first-stage dephlegmator (15), the top of the first-stage dephlegmator (15) is connected with the middle of a second-stage dephlegmator (17) through a second-stage condenser (16), the top of the second-stage dephlegmator (17) is connected with the middle of a third-stage dephlegmator (19) through a third-stage condenser (18), the bottoms of the first-stage dephlegmator (15) and the second-stage dephlegmator (17) are connected with the middle of a raw material water tank (7) together through a connecting dephlegmator (20), and the top of the third-stage dephlegmator (19) discharges gas;
the bottom of the acid gas separator (11) is connected with the middle part of the raw material water tank (7), and the top of the acid gas separator (11) discharges gas through an acid gas heater (21);
the bottom of the stripping tower b (9) is provided with a purifying water pump b (12), the stripping tower b (9) is connected with a secondary preheater (13) through the purifying water pump b (12) and then is divided into two paths, one path is directly discharged, and the other path is sequentially connected with an acid gas heater (21) and a washing liquid cooler (22) to the top of the stripping tower b (9).
2. The apparatus for recovering ammonia resources from a shift condensate as claimed in claim 1, wherein: and steam is directly introduced into the bottom of the stripping tower b (9) and is used as a heat source of a heating medium.
3. The apparatus for recovering ammonia resources from a shift condensate as claimed in claim 1, wherein: a part of raw water of the raw water tank (7) is dilute ammonia water (5-1) generated by condensation of an original stripping system, and the other part of raw water is conversion condensate and ammonia washing liquid (1-1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321990685.XU CN220467588U (en) | 2023-07-27 | 2023-07-27 | Change condensate ammonia resource recovery unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321990685.XU CN220467588U (en) | 2023-07-27 | 2023-07-27 | Change condensate ammonia resource recovery unit |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220467588U true CN220467588U (en) | 2024-02-09 |
Family
ID=89799232
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321990685.XU Active CN220467588U (en) | 2023-07-27 | 2023-07-27 | Change condensate ammonia resource recovery unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220467588U (en) |
-
2023
- 2023-07-27 CN CN202321990685.XU patent/CN220467588U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4305733A (en) | Method of treating natural gas to obtain a methane rich fuel gas | |
| US4198378A (en) | Process for removing CO2, H2 S and other gaseous impurities from gaseous mixtures | |
| CN110740801A (en) | Method and device for cleaning gas with at least two injection phases and use | |
| CN109399666A (en) | A kind of method and device recycling ammonia from acid water | |
| CN114634400A (en) | Method and production system for synthesizing methanol by using carbon dioxide | |
| CN111847478B (en) | Comprehensive treatment process for conversion condensate | |
| CN102060662A (en) | Chemical power poly-generation energy system and method for recycling CO2 | |
| US3709976A (en) | Gas desulfurization process | |
| CN211782272U (en) | Carbon dioxide rectification separation waste liquid treatment device | |
| CN220467588U (en) | Change condensate ammonia resource recovery unit | |
| CN102320568A (en) | Method and device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation | |
| CN209854029U (en) | Device for preparing methanol from synthesis gas without conversion system | |
| CN112239682A (en) | Gasification device slag water flash evaporation gas comprehensive utilization system and method | |
| CN110342717A (en) | Gasification energy couples ammonia recovery system and method | |
| US4620967A (en) | Method of recovering sulfur in a Claus process from vapors obtained in coke oven gas cleaning | |
| CN215886928U (en) | Purification system of raw gas | |
| CN202208705U (en) | Device for preparing synthesis gas or hydrogen through BGL pressurizing molten slag gasification with pure oxygen non-catalytic partial oxidation | |
| CN220758035U (en) | High-efficient ammonia stripping device of transform lime set single tower | |
| CN104030316A (en) | Novel process for producing anhydrous ammonia from raw gas | |
| CN114906897B (en) | Coking wastewater ammonia distillation treatment device and process method | |
| CN215403099U (en) | Production system for preparing sulfuric acid from coke oven gas desulfurization waste liquid and sulfur foam | |
| CN108249501B (en) | Coal gas water treatment system of Lurgi furnace gasification anthracite device | |
| CN220214868U (en) | Novel phenol acetone tar efficient utilization system | |
| CN220467589U (en) | Device for preparing superior ammonia water from crude ammonia gas | |
| CN219128824U (en) | Sulfur production tail gas treatment equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |