CN216712018U - Vacuum carbonate desulfurization pregnant solution desorption system - Google Patents
Vacuum carbonate desulfurization pregnant solution desorption system Download PDFInfo
- Publication number
- CN216712018U CN216712018U CN202123358221.0U CN202123358221U CN216712018U CN 216712018 U CN216712018 U CN 216712018U CN 202123358221 U CN202123358221 U CN 202123358221U CN 216712018 U CN216712018 U CN 216712018U
- Authority
- CN
- China
- Prior art keywords
- desulfurization
- liquid
- gas
- solution
- barren
- 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
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model relates to a vacuum carbonate desulfurization pregnant solution desorption system, which comprises a desulfurization pregnant solution desorption tower, a 1# gas-liquid separator, a supercharger, a 1# reboiler, a 2# gas-liquid separator, an acid gas cooler, a 3# gas-liquid separator, a vacuum pump, a reflux liquid pump, a barren and pregnant solution heat exchanger, a barren liquid cooler and a 2# reboiler; the acid steam at the top of the desulfurization pregnant solution desorption tower is pressurized by the booster to increase the temperature of the acid steam, and the pressurized and heated acid steam is used as a heat source of the desulfurization pregnant solution desorption tower, so that the latent heat of the water vapor in the acid steam at the top of the tower is fully utilized; the equipment investment is low, the operation cost is low, the process flow is simple, and the high-efficiency energy-saving improvement of the vacuum carbonate desulfurization pregnant solution desorption process is realized.
Description
Technical Field
The utility model relates to the technical field of gas purification and desulfurization, in particular to a high-efficiency and energy-saving vacuum carbonate desulfurization pregnant solution desorption system.
Background
The vacuum potassium carbonate desulfurization process is generally installed at the end of the coke oven gas purification process. The vacuum potassium carbonate method desulfurization technology is to use potassium carbonate solution to directly absorb H in coal gas2S and HCN. The sulfur-containing coal gas is in countercurrent contact with barren liquor (potassium carbonate solution) through a carbonate desulfurizing tower to absorb acid gas H in the coal gas2S, HCN, the desulfurization rich liquid is sent to the desorption tower to carry out desulfurization desorption regeneration. The desorption tower operates under negative pressure, the desulfurization rich solution is in countercurrent contact with desorption steam rising at the bottom of the desorption tower, so that the acid gas is desorbed from the desulfurization rich solution, and the desorbed barren solution is sent to the desulfurization tower for recycling. The product of the vacuum potassium carbonate method desulfurization process is H-containing2The acid steam with higher S and HCN concentration can be further sent to a sulfur recovery unit or an acid making unit for recycling.
At present, in the coking industry, the vacuum carbonate desulfurization process mostly adopts a stripping method to be matched with a larger vacuum degree to carry out desulfurization pregnant solution desorption so as to increase H2Removal rate of S and HCN. However, the energy consumption for regenerating the desulfurization rich solution by adopting a stripping method is high, so that how to improve the energy utilization rate in the desorption process of the vacuum carbonate desulfurization rich solution and reduce the energy unit consumption becomes a problem which is generally concerned by technical personnel in the industry.
The utility model discloses a Chinese utility model patent with the publication number of CN 100560698C, which discloses a vacuum carbonate method gas desulfurization process and equipment thereof, wherein the waste heat of raw gas is directly used as a desorption heat source, the waste heat of raw gas is used for providing a heat source for desorption of rich liquid in vacuum carbonate desulfurization, the specific mode is that a heat exchange section is arranged on the upper section of a primary cooler, coke oven gas with the temperature of about 80 ℃ is used for forced circulation heat exchange for the lean liquid at the bottom of the carbonate desulfurization desorption tower in the heat exchange section on the upper section of the primary cooler, and most or all heat sources are provided for the steam stripping regeneration process of the rich liquid in carbonate desulfurization; the method integrates most of low-grade waste heat of the coking plant, and greatly saves the energy consumption in the desorption process of the vacuum carbonate desulfurization pregnant solution. However, although the process utilizes the waste heat of the raw gas in the process of vacuum carbonate desulfurization desorption, the energy consumption efficiency of the carbonate desulfurization pregnant solution desorption process is not improved, and the consumption of circulating water is still large. When a coke-oven plant adopts a vacuum carbonate desulfurization process, most of the waste heat of the raw gas is used for the desorption process of the desulfurization rich liquor, and the waste heat can be used in places such as a refrigeration system in the plant and the like which can utilize low-quality waste heat, so that the process cannot really reduce the energy consumption of the plant.
The utility model discloses a chinese utility model patent of grant publication No. CN 104629818B discloses a "desulfurization rich liquid double effect desorption process and system by vacuum carbonate method", adopts the latent heat of tower top ammonia vapor in the ammonia distillation process as the partial heat source of desorption of the desulfurization rich liquid of vacuum carbonate, and it has integrated partial low-grade waste heat of coke-oven plant, has improved the energy utilization ratio of mill self. But the waste heat quantity which can be utilized by the technique only accounts for about 19 percent of the heat quantity used at the bottom of the vacuum carbonate desulfurization pregnant solution desorption tower, and the energy consumption of the vacuum carbonate desulfurization pregnant solution desorption technique is still higher.
Disclosure of Invention
The utility model provides a vacuum carbonate desulfurization pregnant solution desorption system, which adopts a supercharger to pressurize acid steam at the top of a desulfurization pregnant solution desorption tower so as to increase the temperature of the acid steam, and then uses the pressurized and heated acid steam as a heat source of the desulfurization pregnant solution desorption tower, thereby fully utilizing the latent heat of water vapor in the acid steam at the top of the tower; the equipment investment is low, the operation cost is low, the process flow is simple, and the high-efficiency energy-saving improvement of the vacuum carbonate desulfurization pregnant solution desorption process is realized.
In order to achieve the purpose, the utility model adopts the following technical scheme:
a vacuum carbonate desulfurization pregnant solution desorption system comprises a desulfurization pregnant solution desorption tower, a 1# gas-liquid separator, a supercharger, a 1# reboiler, a 2# gas-liquid separator, an acid gas cooler, a 3# gas-liquid separator, a vacuum pump, a reflux pump, a barren liquor pump, a barren and pregnant solution heat exchanger, a barren liquor cooler and a 2# reboiler; the No. 1 reboiler and the No. 2 reboiler are arranged on two sides of the bottom of the desulfurization rich liquid desorption tower and are respectively connected with the desulfurization rich liquid desorption tower through corresponding desulfurization lean liquid circulating pipelines;
the upper part of the desulfurization rich solution desorption tower is provided with a desulfurization rich solution inlet which is connected with a desulfurization rich solution pipeline, and the desulfurization rich solution pipeline is provided with a lean rich solution heat exchanger; a desulfurization barren solution inlet of the barren and rich solution heat exchanger is connected with a desulfurization barren solution outlet at the bottom of the desulfurization rich solution desorption tower through a barren solution inlet pipe, and a barren solution pump is arranged on the barren solution inlet pipe; a desulfurization barren solution outlet of the barren and rich solution heat exchanger is connected with a desulfurization barren solution inlet on the desulfurizing tower through a barren solution outlet pipe, and a barren solution cooler is arranged on the barren solution outlet pipe;
the top of the desulfurization rich liquid desorption tower is provided with an acid gas outlet pipe which is connected with a gas-liquid mixture inlet of the No. 1 gas-liquid separator, and a liquid phase outlet of the No. 1 gas-liquid separator is connected with a liquid phase inlet at the upper part of the desulfurization rich liquid desorption tower through a pipeline; the vapor phase outlet of the No. 1 vapor-liquid separator is connected with the heat source inlet of the No. 1 reboiler through a pipeline, and a supercharger is arranged on the corresponding pipeline; a heat source outlet of the 1# reboiler is connected with a vapor-liquid mixture inlet of the 2# vapor-liquid separator through a pipeline;
a liquid phase outlet of the No. 2 gas-liquid separator is connected with a reflux inlet at the upper part of the desulfurization rich liquid desorption tower through a pipeline, and a reflux pump is arranged on the corresponding pipeline; the gas-phase outlet of the No. 2 gas-liquid separator is connected with the gas-liquid mixture inlet of the No. 3 gas-liquid separator through a pipeline, and an acid gas cooler is arranged on the corresponding pipeline;
the liquid phase outlet of the No. 3 vapor-liquid separator is connected with the liquid phase inlet of the No. 2 vapor-liquid separator through a pipeline; the vapor phase outlet of the No. 3 vapor-liquid separator is connected with an external sulfur recovery unit or an acid making unit through a pipeline, and a vacuum pump is arranged on the corresponding pipeline;
and the heat source inlet of the 2# reboiler is connected with an external heat source pipeline.
Compared with the prior art, the utility model has the beneficial effects that:
(1) the energy consumption is greatly reduced:
compared with the traditional vacuum carbonate desulfurization pregnant solution desorption technology, the technology of the utility model is adopted to carry out carbonate desulfurization pregnant solutionIn the aspect of waste heat water consumption or steam consumption, temporary steam or waste heat water is only needed to be added during start-up, and less waste heat water or steam is only consumed during normal production operation, so that about 75% of waste heat water consumption or steam consumption is saved; in the aspect of circulating water consumption, the circulating water consumption is saved by about 81.5 percent; in the aspect of electric energy consumption, the newly increased electric energy consumption is only 0.009 DEG/Nm3Coal gas; the total operation cost can be reduced by 68-81%.
(2) The equipment investment is small:
compared with the prior art, only equipment such as a supercharger, a reboiler, a gas-liquid separator, a reflux pump and the like are added, but an acid gas condensation cooler in the traditional vacuum carbonate desulfurization pregnant solution desorption system is saved;
(3) the process flow is simple, the operation is convenient, and the operation cost is low.
Drawings
FIG. 1 is a schematic structural diagram of a vacuum carbonate desulfurization pregnant solution desorption system according to the present invention.
In the figure: 1. 2.1# gas-liquid separator 3 of desulfurization rich solution desorption tower, 4.1# reboiler 5.2# gas-liquid separator 6 of booster, 7.3# gas-liquid separator 8 of acid gas cooler, 9 vacuum pump, 10 reflux pump, 11 lean solution pump, 12 lean rich solution heat exchanger, 13.2# reboiler of lean solution cooler
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in fig. 1, the vacuum carbonate desulfurization rich solution desorption system comprises a desulfurization rich solution desorption tower 1, a # 1 vapor-liquid separator 2, a supercharger 3, a # 1 reboiler 4, a # 2 vapor-liquid separator 5, an acid gas cooler 6, a # 3 vapor-liquid separator 7, a vacuum pump 8, a reflux liquid pump 9, a lean liquid pump 10, a lean and rich solution heat exchanger 11, a lean liquid cooler 12 and a # 2 reboiler 13; the 1# reboiler 4 and the 2# reboiler 13 are arranged on two sides of the bottom of the desulfurization rich solution desorption tower 1 and are respectively connected with the desulfurization rich solution desorption tower 1 through corresponding desulfurization lean solution circulating pipelines;
a desulfurization rich solution inlet is arranged at the upper part of the desulfurization rich solution desorption tower 1 and is connected with a desulfurization rich solution pipeline, and a lean rich solution heat exchanger 11 is arranged on the desulfurization rich solution pipeline; a desulfurization barren solution inlet of the barren and rich solution heat exchanger 11 is connected with a desulfurization barren solution outlet at the bottom of the desulfurization barren solution desorption tower 1 through a barren solution inlet pipe, and a barren solution pump 10 is arranged on the barren solution inlet pipe; a desulfurization barren solution outlet of the barren and rich solution heat exchanger 11 is connected with a desulfurization barren solution inlet on the desulfurizing tower through a barren solution outlet pipe, and a barren solution cooler 12 is arranged on the barren solution outlet pipe;
an acid gas outlet pipe is arranged at the top of the desulfurization rich liquid desorption tower 1 and is connected with a gas-liquid mixture inlet of the No. 1 gas-liquid separator 2, and a liquid phase outlet of the No. 1 gas-liquid separator 2 is connected with a liquid phase inlet at the upper part of the desulfurization rich liquid desorption tower 1 through a pipeline; a vapor phase outlet of the No. 1 vapor-liquid separator 2 is connected with a heat source inlet of a No. 1 reboiler 4 through a pipeline, and a supercharger 3 is arranged on the corresponding pipeline; a heat source outlet of the 1# reboiler 4 is connected with a vapor-liquid mixture inlet of the 2# vapor-liquid separator 5 through a pipeline;
a liquid phase outlet of the 2# vapor-liquid separator 5 is connected with a reflux liquid inlet at the upper part of the desulfurization rich liquid desorption tower 1 through a pipeline, and a reflux liquid pump 9 is arranged on the corresponding pipeline; a vapor phase outlet of the No. 2 vapor-liquid separator 5 is connected with a vapor-liquid mixture inlet of the No. 3 vapor-liquid separator 7 through a pipeline, and an acid vapor cooler 6 is arranged on the corresponding pipeline;
a liquid phase outlet of the No. 3 vapor-liquid separator 7 is connected with a liquid phase inlet of the No. 2 vapor-liquid separator 5 through a pipeline; the vapor phase outlet of the 3# vapor-liquid separator 7 is connected with an external sulfur recovery unit or an acid making unit through a pipeline, and a vacuum pump 8 is arranged on the corresponding pipeline;
the heat source inlet of the 2# reboiler 13 is connected with an external heat source pipeline.
The utility model relates to a vacuum carbonate desulfurization pregnant solution desorption system, which is an efficient energy-saving system and has the working principle that: the desulfurization rich solution is heated by a lean rich solution heat exchanger 11 and then enters the top of a desulfurization rich solution desorption tower 1 for desorption, acid gas at the top of the tower is pressurized and heated by a supercharger 8 after entrained liquid drops are removed, and then enters a tower bottom reboiler for heat exchange with the desulfurization lean solution, so that most of heat required by the desorption of the desulfurization rich solution is provided; the rest small amount of heat required by the desorption operation of the desulfurization rich solution is provided by an external heat source (such as residual heat water, low-pressure steam and the like).
The technological process of the vacuum carbonate desulfurization pregnant solution desorption system comprises the following steps:
(1) after exchanging heat with the desulfurized barren solution drawn out from the bottom of the desulfurized rich solution desorption tower 1 through the barren rich solution heat exchanger 11, the desulfurized rich solution of the carbonate enters the top of the desulfurized rich solution desorption tower 1 for desorption;
(2) acid gas at the top of the desulfurization rich liquid desorption tower 1 enters a No. 1 gas-liquid separator 2 to remove liquid drops carried by gas phase gas flow, a separated liquid phase enters the top of the desulfurization rich liquid desorption tower 1 under the action of gravity, and the separated gas phase is pressurized and heated by a supercharger 3;
(3) the acid steam is pressurized and heated, then enters a reboiler No. 1 at the bottom of the desulfurization rich liquid desorption tower 1, and exchanges heat with the desulfurization lean liquid at the bottom of the desulfurization rich liquid desorption tower 1 to form a steam-liquid mixture I, so that most of heat is provided for desorption of the desulfurization rich liquid, and the rest of heat is provided by an external heat source;
(4) the gas-liquid mixture I from the 1# reboiler 4 enters a 2# gas-liquid separator 5 for gas-liquid separation, the separated liquid phase enters the top of the desulfurization rich liquid desorption tower 1 through a reflux pump 9, and the separated vapor phase enters an acid gas cooler 6 and is cooled into a gas-liquid mixture II by circulating water;
(5) the gas-liquid mixture II from the acid gas cooler 6 enters a 3# gas-liquid separator 7 for gas-liquid separation again, the separated liquid phase enters a 2# gas-liquid separator 5 under the action of gravity, and the separated gas-phase acid gas enters a vacuum pump 8 and is pumped to a sulfur recovery unit or an acid making unit;
(6) the desulfurization barren liquor at the bottom of the desulfurization barren liquor desorption tower 1 is extracted by a barren liquor pump 10, exchanges heat with the desulfurization barren liquor before entering the desulfurization barren liquor desorption tower 1 through a barren liquor heat exchanger 11, is cooled by low-temperature water through a barren liquor cooler 12, and is sent to the desulfurization tower for desulfurization;
(7) and (3) exchanging heat between an external heat source and the desulfurization lean solution at the bottom of the desulfurization rich solution desorption tower 1 through a No. 2 reboiler 13 to provide the rest small part of heat in the step (3) for desorption of the desulfurization rich solution.
In the step (1), the temperature of the carbonate desulfurization pregnant solution after heat exchange with the desulfurization barren solution is 45-55 ℃; the top pressure of the desulfurization rich liquid desorption tower 1 is-88 kPag to-75 kPag, and the tower top temperature is 50-65 ℃.
In the step (2), the acid gas discharge pressure at the outlet of the supercharger 3 is-68 kPag to-55 kPag.
In the step (3), the temperature of the first vapor-liquid mixture is 62-72 ℃.
In the step (4), the temperature of the vapor-liquid mixture II is 33-40 ℃.
In the step (5), the acid steam extraction pressure at the inlet of the vacuum pump is-74 kPag to-54 kPag; the acid steam discharge pressure of the vacuum pump outlet is 15 kPag-40 kPag.
In the step (6), the temperature of the desulfurized barren solution cooled by the low-temperature water is 25-35 ℃.
The external heat source is low-pressure steam or waste heat water of a primary cooler.
The following examples are carried out on the premise of the technical scheme of the utility model, and detailed embodiments and specific operation processes are given, but the scope of the utility model is not limited to the following examples.
[ example 1 ]
In this embodiment, to process 100000Nm3For example, the rich solution is desorbed in vacuum potassium carbonate desulfurization of coke oven gas (dry gas), and the content of impurities in the coke oven gas is as follows: h2S 7.5g/Nm3Vacuum potassium carbonate desulfurization purge to 200mg/Nm3。
After heat exchange between the carbonate desulfurization rich solution subjected to vacuum potassium carbonate desulfurization and a desulfurization barren solution extracted from the bottom of a desulfurization rich solution desorption tower is carried out to 50 ℃, the carbonate desulfurization rich solution enters the top of the desulfurization rich solution desorption tower to carry out desorption operation; the temperature at the top of the desulfurization rich solution desorption tower is 58 ℃, and the pressure is-84 kPag; the bottom temperature of the desulfurization rich solution desorption tower is 61 ℃, and the pressure is-82 kPag.
Acid gas at the top of the desulfurization rich liquid desorption tower enters a No. 1 gas-liquid separator to remove liquid drops carried by gas flow of a gas phase, a separated liquid phase enters the top of the desulfurization rich liquid desorption tower under the action of gravity, and the separated gas phase is pressurized by a supercharger and heated to-64 kPag and 75 ℃ and then enters a No. 1 reboiler at the bottom of the desulfurization rich liquid desorption tower to exchange heat with desulfurization lean liquid at the bottom of the self-desulfurization rich liquid desorption tower to form a gas-liquid mixture I with the temperature of 69 ℃ so as to provide most of heat for the desorption of the desulfurization rich liquid.
The first gas-liquid mixture with the temperature of 69 ℃ enters a No. 2 gas-liquid separator for gas-liquid separation, the separated liquid phase enters the top of a desulfurization rich liquid desorption tower through a reflux pump, the separated gas phase enters an acid gas cooler, and enters a No. 3 gas-liquid separator for gas-liquid separation again after being cooled to 40 ℃ by circulating water; the separated liquid phase enters a No. 2 vapor-liquid separator under the action of gravity, the separated vapor phase (acid vapor) enters a vacuum pump, the vacuum pump sucks the acid vapor to generate negative pressure of-65 kPag, and the sucked acid vapor is pressurized by the vacuum pump, heated to 30kPag and 40 ℃ and then sent to a sulfur recovery unit or an acid preparation unit.
And pumping the desulfurization barren solution at the bottom of the desulfurization rich solution desorption tower by a barren solution pump, exchanging heat with the desulfurization rich solution to 37 ℃, then cooling the desulfurization barren solution in a barren solution cooler to 28 ℃ by low-temperature water, and then sending the desulfurization barren solution to a potassium carbonate desulfurization tower for desulfurization.
The rest small amount of heat required by the operation of the desulfurization rich solution desorption tower is provided by low-pressure steam, and the low-pressure steam exchanges heat with the desulfurization lean solution at the bottom of the desulfurization rich solution desorption tower through a 2# reboiler, so that the small amount of heat is provided for the desorption of the desulfurization rich solution.
In example 1, the content of potassium carbonate in the desulfurized lean solution at the bottom of the desulfurization rich solution desorption tower is about 80 g/L.
[ example 2 ]
In this embodiment, to process 100000Nm3For example, the rich solution is desorbed in vacuum potassium carbonate desulfurization of coke oven gas (dry gas), and the content of impurities in the coke oven gas is as follows: h2S 7.5g/Nm3Vacuum potassium carbonate desulfurization purge to 200mg/Nm3。
After heat exchange between the carbonate desulfurization rich solution subjected to vacuum potassium carbonate desulfurization and a desulfurization barren solution extracted from the bottom of a desulfurization rich solution desorption tower is carried out to 50 ℃, the carbonate desulfurization rich solution enters the top of the desulfurization rich solution desorption tower to carry out desorption operation; the temperature at the top of the desulfurization rich solution desorption tower is 58 ℃, and the pressure is-84 kPag; the bottom temperature of the desulfurizing pregnant solution desorption tower is 61 ℃, and the pressure is-82 kPag.
Acid gas at the top of the desulfurization rich liquid desorption tower enters a No. 1 gas-liquid separator to remove liquid drops carried by gas-phase gas flow, separated liquid phase enters the top of the desulfurization rich liquid desorption tower under the action of gravity, and separated gas phase is pressurized by a supercharger, heated to-64 kPag and 75 ℃, enters a No. 1 reboiler at the bottom of the desulfurization rich liquid desorption tower, exchanges heat with desulfurization lean liquid at the bottom of the desulfurization rich liquid desorption tower to form a gas-liquid mixture I with the temperature of 69 ℃, and provides most heat for the desorption of the desulfurization rich liquid.
The first gas-liquid mixture with the temperature of 69 ℃ enters a No. 2 gas-liquid separator for gas-liquid separation, the separated liquid phase enters the top of a desulfurization rich liquid desorption tower through a reflux pump, the separated gas phase enters an acid gas cooler, and enters a No. 3 gas-liquid separator for gas-liquid separation again after being cooled to 40 ℃ by circulating water; the separated liquid phase enters a No. 2 vapor-liquid separator under the action of gravity, the separated vapor phase (acid vapor) enters a vacuum pump, the vacuum pump sucks the acid vapor to generate negative pressure of-65 kPag, and the sucked acid vapor is pressurized by the vacuum pump, heated to 30kPag and 40 ℃ and then sent to a sulfur recovery unit or an acid preparation unit.
And pumping the desulfurization barren solution at the bottom of the desulfurization rich solution desorption tower by a barren solution pump, exchanging heat with the desulfurization rich solution to 37 ℃, then cooling the desulfurization barren solution in a barren solution cooler to 28 ℃ by low-temperature water, and then sending the desulfurization barren solution to a potassium carbonate desulfurization tower for desulfurization.
The rest small amount of heat required by the operation of the desulfurization rich solution desorption tower is provided by primary cooler waste heat water (the temperature is 73-63 ℃), and the primary cooler waste heat water exchanges heat with the desulfurization lean solution at the bottom of the desulfurization rich solution desorption tower through a 2# reboiler, so that a small amount of heat is provided for the desorption of the desulfurization rich solution.
In example 2, the content of potassium carbonate in the desulfurized lean solution at the bottom of the desulfurization rich solution desorption tower is about 80 g/L.
The economic benefit analysis of the vacuum carbonate desulfurization pregnant solution desorption system comprises the following steps:
to process H2The S content was 7.5g/Nm3100000Nm3The coke oven gas (dry gas) and the vacuum potassium carbonate are desulfurized and purified to 200mg/Nm3The desorption of the desulfurization rich solution is taken as an example, and the energy consumption comparison of three vacuum hydrochloride desulfurization rich solution desorption systems is detailed in table 1.
TABLE 1 energy consumption benefit comparison of three vacuum potassium hydrochloride desulfurization pregnant solution desorption systems
As can be seen from Table 1: compared with the common conventional vacuum hydrochloride desulfurization rich solution desorption system applied at present, the vacuum carbonate desulfurization rich solution desorption system has the advantages that the total operation cost is reduced by 68-81%, the energy consumption of the vacuum hydrochloride desulfurization rich solution desorption system of enterprises such as coking and the like is greatly reduced, and the problem of high energy consumption of the conventional vacuum carbonate desulfurization unit is fundamentally solved.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and equivalent alternatives or modifications according to the technical solution of the present invention and the inventive concept thereof should be covered by the scope of the present invention.
Claims (1)
1. A vacuum carbonate desulfurization pregnant solution desorption system is characterized by comprising a desulfurization pregnant solution desorption tower, a 1# gas-liquid separator, a supercharger, a 1# reboiler, a 2# gas-liquid separator, an acid gas cooler, a 3# gas-liquid separator, a vacuum pump, a reflux liquid pump, a barren and pregnant solution heat exchanger, a barren solution cooler and a 2# reboiler; the No. 1 reboiler and the No. 2 reboiler are arranged on two sides of the bottom of the desulfurization rich liquid desorption tower and are respectively connected with the desulfurization rich liquid desorption tower through corresponding desulfurization lean liquid circulating pipelines;
the upper part of the desulfurization rich solution desorption tower is provided with a desulfurization rich solution inlet which is connected with a desulfurization rich solution pipeline, and the desulfurization rich solution pipeline is provided with a lean rich solution heat exchanger; a desulfurization barren solution inlet of the barren and rich solution heat exchanger is connected with a desulfurization barren solution outlet at the bottom of the desulfurization rich solution desorption tower through a barren solution inlet pipe, and a barren solution pump is arranged on the barren solution inlet pipe; a desulfurization barren solution outlet of the barren and rich solution heat exchanger is connected with a desulfurization barren solution inlet on the desulfurizing tower through a barren solution outlet pipe, and a barren solution cooler is arranged on the barren solution outlet pipe;
the top of the desulfurization rich liquid desorption tower is provided with an acid gas outlet pipe which is connected with a gas-liquid mixture inlet of the No. 1 gas-liquid separator, and a liquid phase outlet of the No. 1 gas-liquid separator is connected with a liquid phase inlet at the upper part of the desulfurization rich liquid desorption tower through a pipeline; the vapor phase outlet of the No. 1 vapor-liquid separator is connected with the heat source inlet of the No. 1 reboiler through a pipeline, and a supercharger is arranged on the corresponding pipeline; a heat source outlet of the 1# reboiler is connected with a vapor-liquid mixture inlet of the 2# vapor-liquid separator through a pipeline;
a liquid phase outlet of the No. 2 gas-liquid separator is connected with a reflux inlet at the upper part of the desulfurization rich liquid desorption tower through a pipeline, and a reflux pump is arranged on the corresponding pipeline; the gas-phase outlet of the No. 2 gas-liquid separator is connected with the gas-liquid mixture inlet of the No. 3 gas-liquid separator through a pipeline, and an acid gas cooler is arranged on the corresponding pipeline;
the liquid phase outlet of the No. 3 vapor-liquid separator is connected with the liquid phase inlet of the No. 2 vapor-liquid separator through a pipeline; the vapor phase outlet of the No. 3 vapor-liquid separator is connected with an external sulfur recovery unit or an acid making unit through a pipeline, and a vacuum pump is arranged on the corresponding pipeline;
and the heat source inlet of the 2# reboiler is connected with an external heat source pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123358221.0U CN216712018U (en) | 2021-12-29 | 2021-12-29 | Vacuum carbonate desulfurization pregnant solution desorption system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123358221.0U CN216712018U (en) | 2021-12-29 | 2021-12-29 | Vacuum carbonate desulfurization pregnant solution desorption system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216712018U true CN216712018U (en) | 2022-06-10 |
Family
ID=81887240
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202123358221.0U Active CN216712018U (en) | 2021-12-29 | 2021-12-29 | Vacuum carbonate desulfurization pregnant solution desorption system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216712018U (en) |
-
2021
- 2021-12-29 CN CN202123358221.0U patent/CN216712018U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105013296B (en) | A kind of selexol process decarbonization system and method for coupling acid gas concentrate | |
| CN109999618B (en) | System and method for separating carbon dioxide from medium-high pressure gas source | |
| CN102225297B (en) | Heat pump regeneration process for desulphurization solvent used in flue gas desulphurization by solvent cyclic absorption method | |
| CN106673014A (en) | Process of removing sulfur and ammonia from coke gas to prepare ammonia water | |
| CN106479578B (en) | A kind of acid gas removal technique of mating coal gasification | |
| CN108129254A (en) | A kind of device and method of the carbon dioxide removal from ethane gas | |
| US20210106943A1 (en) | Method for recovering co2 in the rectisol process and recovery system | |
| CN104307341B (en) | A kind of torch gas compression and sulfur removal technology | |
| CN105749728B (en) | Method and apparatus for capturing carbon dioxide | |
| CN216712018U (en) | Vacuum carbonate desulfurization pregnant solution desorption system | |
| CN1872679A (en) | Method for preparing liquid carbon dioxide in foodstuff level by using tail gas of cement kiln | |
| CN104056462A (en) | Heat pump distillation energy-saving device | |
| CN219449378U (en) | Energy-saving deacidification ammonia distillation device | |
| CN207811623U (en) | A kind of device of the carbon dioxide removal from ethane gas | |
| CN114133959A (en) | Vacuum carbonate desulfurization pregnant solution desorption process and system | |
| CN116751613A (en) | Energy-saving negative pressure debenzolization process and system | |
| CN218544490U (en) | Flue gas waste heat recovery device of coupling carbon entrapment | |
| CN110639335A (en) | Energy-saving method and system for regeneration tower in deep decarburization of natural gas | |
| CN203989925U (en) | A kind of heat pump distillation energy saver | |
| CN210410096U (en) | Separation system for carbon dioxide in medium-high pressure gas source | |
| CN114212850B (en) | Efficient energy-saving type thermal coupling ammonia distillation process | |
| CN205965520U (en) | Desorption system of desulfurization vacuum condensation liquid | |
| CN117797606A (en) | Energy-saving desorption method and device for vacuum carbonate desulfurization rich liquid | |
| CN105289215B (en) | Flue gas circulation desulfuration method and system | |
| CN217464095U (en) | Low-pressure gas energy-saving consumption-reducing recycling device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |