CN209778320U - System for coupling heat of pressurization deacidification ammonia distillation - Google Patents
System for coupling heat of pressurization deacidification ammonia distillation Download PDFInfo
- Publication number
- CN209778320U CN209778320U CN201920189231.XU CN201920189231U CN209778320U CN 209778320 U CN209778320 U CN 209778320U CN 201920189231 U CN201920189231 U CN 201920189231U CN 209778320 U CN209778320 U CN 209778320U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- inlet
- tower
- outlet
- deacidification
- 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.)
- Withdrawn - After Issue
Links
Landscapes
- Physical Water Treatments (AREA)
Abstract
The utility model relates to a system for coupling heat of pressurized deacidification and ammonia distillation, which comprises a deacidification tower, an ammonia distillation tower, a pump, a condenser, a heat exchanger, a reboiler and a valve; the top of the deacidification tower is provided with an acid gas outlet, the upper part of the deacidification tower is provided with a mixed liquid inlet, the middle part of the deacidification tower is provided with a lean liquid side draw outlet, the lower part of the deacidification tower is provided with an ammonia evaporation gas inlet and a gas-liquid phase return port, and the bottom of the deacidification tower is provided with an ammonia water outlet; the top of the ammonia still is provided with an ammonia still gas outlet, the upper part of the ammonia still is provided with an ammonia water inlet and a condensate inlet, the middle part of the ammonia still is provided with an alkali liquor inlet, and the bottom of the ammonia still is provided with a gas-liquid phase inlet and an ammonia still wastewater outlet; the utility model discloses when guaranteeing rich solution desorption pressure and can realizing the recovery of substep desorption completion ammonia product, further improve ammonia still top of the tower pressure, make ammonia still top of the tower temperature be higher than deacidification tower bottom temperature, carry out the heat coupling through reasonable temperature system for deacidification tower bottom heat supply with ammonia still top of the tower condenser's heat to reach energy saving and emission reduction's purpose.
Description
Technical Field
the utility model relates to a coke oven gas purifies technical field, especially relates to a system of pressurization deacidification ammonia distillation heat coupling.
Background
The ammonia-water desulphurization process is a common process for removing hydrogen sulfide in raw gas. The process takes ammonia in the coal gas as an alkali source, takes an ammonia-containing water solution as a washing medium, and adopts an ammonia-sulfur combined washing (absorption) process to remove hydrogen sulfide in the coal gas. The method comprises a washing device and an ammonia deacidification and distillation device which form a main absorption and desorption process body, and the ammonia and hydrogen sulfide washing and stripping desorption devices are tightly combined together. In the absorption unit, the deacidification ammonia still returns the deacidification lean solution with high ammonia content and the stripping water to absorb ammonia and hydrogen sulfide in the raw gas, so that rich solution containing ammonia and hydrogen sulfide is formed, and the purpose of removing hydrogen sulfide in the raw gas is achieved. In the desorption unit, the deacidified barren solution and stripped water (part of ammonia distillation wastewater) obtained by desorbing the rich solution by the deacidification and ammonia distillation device are sent back to the washing device for recycling.
Compared with other desulfurization processes, the ammonia desulfurization process only uses water as a washing medium and ammonia in the coal gas as an alkali source, does not generate desulfurization waste liquid, and has the advantages of short total coal gas purification process and low investment. However, in the prior art, a desorption unit (deacidification and ammonia distillation) desorbs ammonia gas and hydrogen sulfide together, and the desorbed gas is decomposed by ammonia and then subjected to sulfur recovery. In this process, ammonia, which can be a final chemical product, is directly decomposed as an impurity and is not effectively recovered. Meanwhile, the energy consumption and the operation cost are high in the rich liquid desorption process. Because of the large heat demand at the bottom of the column, the heat is usually supplied by directly introducing steam into the bottom of the column, which also results in the disadvantage of a large amount of waste water from the process.
The deacidification ammonia distillation process matched with the ammonia water method desulfurization process can adopt a process method of pressure deacidification ammonia distillation for effectively recovering ammonia products and increasing the ammonia-sulfur ratio of barren solution. By improving the desorption pressure of the rich solution, the quality of the barren solution is improved and the desulfurization effect is improved while the ammonia product is recovered through stepwise desorption. However, the process still has the problems of high energy consumption, high operation cost and large amount of waste water.
Disclosure of Invention
The utility model provides a system of pressurization deacidification ammonia still process heat coupling when guaranteeing that rich solution desorption pressure can realize the recovery of substep desorption completion ammonia product, further improves ammonia still tower top of the tower pressure, makes ammonia still tower top of the tower temperature be higher than deacidification tower bottom of the tower temperature, for deacidification tower bottom of the tower heat supply with the heat of ammonia still tower top of the tower condenser, carries out the heat coupling through reasonable temperature system to reach energy saving and emission reduction's purpose.
in order to achieve the above purpose, the utility model adopts the following technical scheme:
a system for coupling heat of pressurized deacidification and ammonia distillation comprises a deacidification tower, an ammonia distillation tower, a pump, a condenser, a heat exchanger, a reboiler and a valve; the top of the deacidification tower is provided with an acid gas outlet, the upper part of the deacidification tower is provided with a mixed liquid inlet, the middle part of the deacidification tower is provided with a lean liquid side draw outlet, the lower part of the deacidification tower is provided with an ammonia evaporation gas inlet and a gas-liquid phase return port, and the bottom of the deacidification tower is provided with an ammonia water outlet; the mixed liquid inlet is connected with a first heat exchange medium outlet of the heat exchanger, and a first heat exchange medium inlet of the heat exchanger is connected with a desulfurizing tower rich liquid conveying pipeline and a residual ammonia water conveying pipeline; a lean solution side outlet of the deacidification tower is connected with a second heat exchange medium inlet of the heat exchanger, and a second heat exchange medium outlet of the heat exchanger is connected with a lean solution conveying pipeline; the top of the ammonia still is provided with an ammonia still gas outlet, the upper part of the ammonia still is provided with an ammonia water inlet and a condensate inlet, the middle part of the ammonia still is provided with an alkali liquor inlet, and the bottom of the ammonia still is provided with a gas-liquid phase inlet and an ammonia still wastewater outlet; an ammonia water outlet of the deacidification tower is connected with an inlet of a pump, an outlet of the pump is respectively connected with an ammonia water inlet of an ammonia still and a first heat exchange medium inlet of a condenser, and a first heat exchange medium outlet of the condenser is connected with a gas-liquid phase return port of the deacidification tower; an ammonia evaporation gas outlet of the ammonia evaporation tower is connected with a second heat exchange medium inlet of the condenser through one pipeline, the ammonia evaporation gas outlet of the ammonia evaporation tower is connected with an ammonia evaporation gas inlet of the deacidification tower through the other pipeline, and a valve is arranged on the pipeline connected with the ammonia evaporation gas inlet; a second heat exchange medium outlet of the condenser is connected with an ammonia product pipeline, and a condensate outlet of the condenser is connected with a condensate inlet of the ammonia still; the ammonia distillation wastewater outlet of the ammonia distillation tower is connected with an ammonia distillation wastewater pipeline, the ammonia distillation wastewater pipeline is connected with an inlet of a reboiler through a branch pipeline, an outlet of the reboiler is connected with a gas-liquid phase inlet of the ammonia distillation tower, and the ammonia distillation wastewater pipeline at the downstream of the branch pipeline is additionally connected with a steam stripping water conveying pipeline.
And the deacidification tower is provided with a plurality of layers of fillers or trays in 2 sections of tower bodies positioned between the mixed liquid inlet and the lean liquid side draw-out port and between the lean liquid side draw-out port and the ammonia distillation gas inlet respectively.
and the ammonia still is provided with a plurality of layers of fillers or trays in 2 sections of tower bodies positioned between the ammonia water inlet and the alkali liquor inlet and between the alkali liquor inlet and the gas-liquid phase inlet.
compared with the prior art, the beneficial effects of the utility model are that:
1) The pressure at the top of the ammonia still is increased, so that the temperature at the top of the ammonia still is higher than the temperature at the bottom of the deacidification tower, and the ammonia still serves as a reboiler of the desulfurization tower to supply heat to the desulfurization tower while the ammonia still is concentrated by a condenser of the ammonia still;
2) By means of heat coupling, the steam consumption of the system is reduced, and meanwhile, the area required by a reboiler at the bottom of the ammonia still is reduced; and the waste water discharge is reduced by adopting a steam indirect heating mode.
Drawings
Fig. 1 is a flow chart of the process of the present invention for coupling heat in the pressurized deacidification and ammonia distillation.
In the figure: 1. the system comprises a deacidification tower 11, an acid gas discharge port 12, a mixed liquid inlet 13, a lean liquid side draw-out port 14, an ammonia distillation gas inlet 15, a gas-liquid phase return port I16, an ammonia water discharge port 2, an ammonia distillation tower 21, an ammonia distillation gas outlet 22, an ammonia water inlet 23, a condensate inlet 24, an alkali liquor inlet 25, a gas-liquid phase inlet 26, an ammonia distillation wastewater outlet 3, a heat exchanger 4, a pump 5, a condenser 6, a reboiler 7 and a valve
Detailed Description
The following description of the embodiments of the present invention will be made with reference to the accompanying drawings:
as shown in fig. 1, the system for coupling heat of pressurized deacidification and ammonia distillation comprises a deacidification tower 1, an ammonia distillation tower 2, a pump 4, a condenser 5, a heat exchanger 3, a reboiler 6 and a valve 7; the top of the deacidification tower 1 is provided with an acid gas outlet 11, the upper part is provided with a mixed liquid inlet 12, the middle part is provided with a lean liquid side draw outlet 13, the lower part is provided with an ammonia distillation gas inlet 14 and a gas-liquid phase return port 15, and the bottom is provided with an ammonia water outlet 16; the mixed liquid inlet 12 is connected with a first heat exchange medium outlet of the heat exchanger 3, and a first heat exchange medium inlet of the heat exchanger 3 is connected with a desulfurizing tower rich liquid conveying pipeline and a residual ammonia water conveying pipeline; a lean solution side outlet 13 of the deacidification tower 1 is connected with a second heat exchange medium inlet of the heat exchanger 3, and a second heat exchange medium outlet of the heat exchanger 3 is connected with a lean solution conveying pipeline; an ammonia distillation gas outlet 21 is formed in the top of the ammonia distillation tower 2, an ammonia water inlet 22 and a condensate inlet 23 are formed in the upper portion of the ammonia distillation tower, an alkali liquor inlet 24 is formed in the middle of the ammonia distillation tower, and a gas-liquid phase inlet 25 and an ammonia distillation wastewater outlet 26 are formed in the bottom of the ammonia distillation tower; an ammonia water outlet 16 of the deacidification tower 1 is connected with an inlet of a pump 4, an outlet of the pump 4 is respectively connected with an ammonia water inlet 22 of the ammonia still 2 and a first heat exchange medium inlet of a condenser 5, and a first heat exchange medium outlet of the condenser 5 is connected with a gas-liquid phase return port 15 of the deacidification tower 1; an ammonia evaporation gas outlet 21 of the ammonia evaporation tower 2 is connected with a second heat exchange medium inlet of the condenser 5 through one pipeline, the ammonia evaporation gas outlet is connected with an ammonia evaporation gas inlet 14 of the deacidification tower 1 through the other pipeline, and a valve 7 is arranged on the pipeline connected with the ammonia evaporation gas inlet 14; a second heat exchange medium outlet of the condenser 5 is connected with an ammonia product pipeline, and a condensate outlet of the condenser 5 is connected with a condensate inlet 23 of the ammonia still 2; an ammonia distillation wastewater outlet 26 of the ammonia distillation tower 2 is connected with an ammonia distillation wastewater pipeline, the ammonia distillation wastewater pipeline is connected with an inlet of a reboiler 6 through a branch pipeline, an outlet of the reboiler 6 is connected with a gas-liquid phase inlet 25 of the ammonia distillation tower 2, and the ammonia distillation wastewater pipeline at the downstream of the branch pipeline is additionally connected with a stripping water conveying pipeline.
The deacidification tower 1 is provided with a plurality of layers of fillers or trays in 2 sections of tower bodies positioned between a mixed liquid inlet 12 and a lean liquid side draw-out port 13 and between the lean liquid side draw-out port 13 and an ammonia distillation gas inlet 14 respectively.
The ammonia still 2 is provided with a plurality of layers of fillers or trays in 2 sections of tower bodies which are positioned between the ammonia water inlet 22 and the alkali liquor inlet 24 and between the alkali liquor inlet 24 and the gas-liquid phase inlet 25 respectively.
The technological process of a system for coupling the heat of ammonia distillation by pressurization and deacidification is as follows:
1) the rich solution from the desulfurizing tower is mixed with the residual ammonia water, and enters the top of the deacidification tower 1 after exchanging heat with the lean solution of the deacidification tower through a heat exchanger 3; the top of the deacidification tower 1 inhibits ammonia from escaping through pressurization operation, so that the acid gas product at the tower top of the deacidification tower 1 only contains a small amount of ammonia;
2) Acid gas escapes from the top of the deacidification tower 1, and barren liquor collected from the side line of the deacidification tower 1 exchanges heat with rich liquor of the desulfurization tower and residual ammonia water and returns to the desulfurization tower for recycling;
3) The pressure at the top of the ammonia still 2 is greater than the pressure at the bottom of the deacidification tower 1, the liquid phase at the bottom of the deacidification tower 1 is pressurized by a pump 4, one part of the liquid phase enters the top of the ammonia still 2 for ammonia distillation treatment, the other part of the liquid phase enters a condenser 5 at the top of the ammonia still 2 for heating, and the heated gas-liquid phase returns to the bottom of the deacidification tower 1;
4) after ammonia evaporation gas at the top of the ammonia still 2 escapes, one part of the ammonia evaporation gas enters a tower top condenser 5 for condensation and concentration treatment, and the other part of the ammonia evaporation gas is adjusted by a valve 7 and returns to the bottom of the deacidification tower 1 to be used as a bottom heat source of the deacidification tower 1;
5) After ammonia evaporation gas at the top of the ammonia still 2 is concentrated by a condenser 5, a gas phase escapes to form an ammonia product, and a liquid phase returns to the ammonia still 2 to be used as reflux;
6) alkali liquor is added into the middle of the ammonia still 2 for removing fixed ammonia, the reboiler 6 provides heat to the bottom of the ammonia still 2, and a part of ammonia still wastewater discharged from the bottom of the ammonia still 2 returns to the desulfurization section to be used as stripping water for desulfurizing and washing ammonia, and simultaneously supplies heat to the desulfurization tower.
The above, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention.
Claims (3)
1. a system for coupling heat of pressurized deacidification and ammonia distillation is characterized by comprising a deacidification tower, an ammonia distillation tower, a pump, a condenser, a heat exchanger, a reboiler and a valve; the top of the deacidification tower is provided with an acid gas outlet, the upper part of the deacidification tower is provided with a mixed liquid inlet, the middle part of the deacidification tower is provided with a lean liquid side draw outlet, the lower part of the deacidification tower is provided with an ammonia evaporation gas inlet and a gas-liquid phase return port, and the bottom of the deacidification tower is provided with an ammonia water outlet; the mixed liquid inlet is connected with a first heat exchange medium outlet of the heat exchanger, and a first heat exchange medium inlet of the heat exchanger is connected with a desulfurizing tower rich liquid conveying pipeline and a residual ammonia water conveying pipeline; a lean solution side outlet of the deacidification tower is connected with a second heat exchange medium inlet of the heat exchanger, and a second heat exchange medium outlet of the heat exchanger is connected with a lean solution conveying pipeline; the top of the ammonia still is provided with an ammonia still gas outlet, the upper part of the ammonia still is provided with an ammonia water inlet and a condensate inlet, the middle part of the ammonia still is provided with an alkali liquor inlet, and the bottom of the ammonia still is provided with a gas-liquid phase inlet and an ammonia still wastewater outlet; an ammonia water outlet of the deacidification tower is connected with an inlet of a pump, an outlet of the pump is respectively connected with an ammonia water inlet of an ammonia still and a first heat exchange medium inlet of a condenser, and a first heat exchange medium outlet of the condenser is connected with a gas-liquid phase return port of the deacidification tower; an ammonia evaporation gas outlet of the ammonia evaporation tower is connected with a second heat exchange medium inlet of the condenser through one pipeline, the ammonia evaporation gas outlet of the ammonia evaporation tower is connected with an ammonia evaporation gas inlet of the deacidification tower through the other pipeline, and a valve is arranged on the pipeline connected with the ammonia evaporation gas inlet; a second heat exchange medium outlet of the condenser is connected with an ammonia product pipeline, and a condensate outlet of the condenser is connected with a condensate inlet of the ammonia still; the ammonia distillation wastewater outlet of the ammonia distillation tower is connected with an ammonia distillation wastewater pipeline, the ammonia distillation wastewater pipeline is connected with an inlet of a reboiler through a branch pipeline, an outlet of the reboiler is connected with a gas-liquid phase inlet of the ammonia distillation tower, and the ammonia distillation wastewater pipeline at the downstream of the branch pipeline is additionally connected with a steam stripping water conveying pipeline.
2. The system for heat coupling of pressure deacidification and ammonia distillation as claimed in claim 1, wherein the deacidification tower is provided with a plurality of layers of packing or trays in 2 sections of tower bodies positioned between the mixed liquid inlet and the lean liquid side draw outlet and between the lean liquid side draw outlet and the ammonia distillation gas inlet respectively.
3. The system for heat coupling of pressurized deacidification and ammonia distillation according to claim 1, wherein the ammonia distillation tower is provided with a plurality of layers of packing or trays in 2 sections of tower bodies positioned between the ammonia water inlet and the alkali liquor inlet and between the alkali liquor inlet and the gas-liquid phase inlet respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920189231.XU CN209778320U (en) | 2019-02-11 | 2019-02-11 | System for coupling heat of pressurization deacidification ammonia distillation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920189231.XU CN209778320U (en) | 2019-02-11 | 2019-02-11 | System for coupling heat of pressurization deacidification ammonia distillation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209778320U true CN209778320U (en) | 2019-12-13 |
Family
ID=68794698
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920189231.XU Withdrawn - After Issue CN209778320U (en) | 2019-02-11 | 2019-02-11 | System for coupling heat of pressurization deacidification ammonia distillation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN209778320U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
-
2019
- 2019-02-11 CN CN201920189231.XU patent/CN209778320U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109704366B (en) | Pressurized deacidification ammonia distillation heat coupling process and system | |
| CN106673014B (en) | Process for preparing ammonia water by desulfurization and deamination of coke oven gas | |
| CN102061197B (en) | Coke oven gas desulfuration and deamination combined purifying method and special device thereof | |
| CN109999618B (en) | System and method for separating carbon dioxide from medium-high pressure gas source | |
| CN105233689B (en) | Organic amine wet flue gas desulphurization and desorption system with high-efficiency and low-energy consumption | |
| CN105195005B (en) | Coking flue gas and ammonia-containing water integrated treatment economic benefits and social benefits cleaning system | |
| CN107754568B (en) | Low-energy-consumption device for capturing and recovering carbon dioxide by flue gas and gas recovery process | |
| CN201990641U (en) | Special device for coke oven gas desulfuration and deamination combined purification method | |
| CN103113928B (en) | Optimization process of vacuum potassium carbonate method coke oven gas desulfurization and equipment thereof | |
| CN202808402U (en) | Residual ammonia water heat pump distillation system | |
| CN209778320U (en) | System for coupling heat of pressurization deacidification ammonia distillation | |
| CN109929638A (en) | A kind of method and apparatus for integrating hydrate and combining acid gas in removing natural gas with hydramine method | |
| CN105236360A (en) | Device and method for improving recycling of low-temperature heat of ore or smelted fume prepared sulfuric acid | |
| CN209771782U (en) | Pressurization deacidification ammonia distillation system | |
| CN110054202B (en) | Process for producing refined ammonia water by deacidifying residual ammonia water | |
| CN203833908U (en) | Natural gas deacidifying device | |
| CN104056462A (en) | Heat pump distillation energy-saving device | |
| CN207998584U (en) | A kind of system for strengthening deacidifion desorption | |
| CN207886919U (en) | Residual neat recovering system | |
| CN210845815U (en) | Energy-conserving efficient deacidification ammonia distillation system | |
| CN109647150A (en) | A kind of pressurization deacidifion technique and system | |
| CN114836246B (en) | Process for purifying coke oven gas and recycling high-quality strong ammonia water and sulfur | |
| CN211159192U (en) | Processing apparatus of acid water is retrieved to claus sulphur | |
| CN108384582B (en) | System and process for strengthening deacidification, ammonia distillation and desorption | |
| CN203612971U (en) | Ammonia distillation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20191213 Effective date of abandoning: 20230801 |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20191213 Effective date of abandoning: 20230801 |