CN213610621U - System for hydrogen sulfide gas is retrieved to high selectivity - Google Patents
System for hydrogen sulfide gas is retrieved to high selectivity Download PDFInfo
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- CN213610621U CN213610621U CN202022615114.0U CN202022615114U CN213610621U CN 213610621 U CN213610621 U CN 213610621U CN 202022615114 U CN202022615114 U CN 202022615114U CN 213610621 U CN213610621 U CN 213610621U
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Abstract
The utility model relates to an industrial gas absorbs the field, concretely relates to system of hydrogen sulfide gas is retrieved to high selectivity, this system is including dividing fluid reservoir, absorption tower, absorbent pregnant solution pump, poor pregnant solution heat exchanger, absorbent barren solution pump, analytic tower, hydrocone type reboiler, cold-trap and compressor. The hydrogen sulfide in the industrial gas is separated out in a high-selectivity manner by adopting a novel high-selectivity hydrogen sulfide absorbent and an absorption and analysis method, so that the high-purity hydrogen sulfide gas is obtained. The system can recover the hydrogen sulfide gas in the industrial gas with high selectivity, and the absorption and the analysis realize continuous production; the difference of the hydrogen sulfide content of the tail gas after absorption is realized through the difference of the absorption stages; the raw material absorbent has extremely low loss, the annual loss rate is 1-2%, and the operation cost is low.
Description
Technical Field
The utility model relates to an industrial gas absorbs the field, concretely relates to system of hydrogen sulfide gas is retrieved to high selectivity.
Background
H2S is a highly toxic corrosive gas which is widely present in industrial gases such as natural gas, synthesis gas, hydrodesulfurization gas and the like. H2The presence of S poses a great threat to the safety and efficiency of the energy utilization process and must therefore be selectively removed from the industrial gas.
H developed in industry2The S removal method can be mainly classified into a dry method and a wet method. The dry method includes a solid adsorption method, a catalytic oxidation method, and the like. The solid adsorption method has simple process and convenient operation, but H2The S removal efficiency is low, the consumption of the adsorbent is high, a large amount of solid waste is easily generated, and serious secondary pollution is caused. The catalytic oxidation method has mature technology, but has long process route, large equipment investment and H-tolerance2Due to thermodynamic limitation of S conversion reaction, the problem of 2-5% of H2S residue in tail gas cannot be solved. The wet method includes physical absorption, chemical absorption, absorption oxidation, etc. Physical absorption method absorbent is easily regenerated, but H2S removal is inefficient and can only be applied at low temperature and high pressure. Chemical absorption of H2The S removal efficiency is high, and the chemical absorbent commonly used in industry is organic alcohol amine, such as ethanolamine (MEA), Diethanolamine (DEA), Methyldiethanolamine (MDEA) and the like. The absorption oxidation method has simple process, but the absorbent is difficult to regenerate, H2The purity of the S conversion product is poor. At present, the wet process H2The mainstream of the S removal technology is still the chemical absorption method of organic alcohol amine. However, the organic alcohol amine is easily volatilized and lost, is easily oxidized and degraded into organic acid to be inactivated, and has high regeneration energy consumption. Therefore, the development of H is urgently required2The method has the advantages of high S removal efficiency, good stability, easy regeneration, environmental protection and energy conservation.
SUMMERY OF THE UTILITY MODEL
In order to overcome the problems, a process system method which obtains high-purity hydrogen sulfide gas through high-selectivity absorption and analysis and recycles an absorbent is provided. The specific system is as follows:
a system for recovering hydrogen sulfide gas with high selectivity comprises: the system comprises a liquid separating tank, an absorption tower, an absorbent pregnant solution pump, a lean pregnant solution heat exchanger, an absorbent lean solution pump, a desorption tower, a siphon reboiler, a cold trap and a compressor;
the liquid separation tank is a jacket double-layer tank, a refrigerant is introduced into the jacket, the temperature of the tank body is kept within 5 ℃, a liquid baffle plate, a demister and a liquid accumulation bag are arranged in the tank body, condensed liquid is collected in the liquid accumulation bag and then discharged, and gas enters the absorption tower through the demister;
the lower part of the absorption tower is provided with a gas inlet to be recovered, the upper part of the absorption tower is provided with an absorbent inlet and a purified gas outlet, the bottom of the absorption tower is provided with an absorbent rich liquid outlet, and the absorbent rich liquid outlet is connected to an absorbent rich liquid pump;
the upper part of the desorption tower is provided with an absorbent rich liquid inlet and a sulfuration hydrogenolysis gas-evolution outlet, the lower part of the desorption tower is connected with the siphon reboiler, and the bottom of the desorption tower is provided with an absorbent lean liquid outlet; the absorbent barren liquor outlet is connected to an absorbent barren liquor pump;
the absorption tower is characterized in that the absorption tower is provided with an absorption tower, an absorption tower is arranged above the absorption tower, an absorption agent rich liquid pump and an absorption agent lean liquid pump are arranged above the absorption tower, and the absorption tower is provided with an absorption agent rich liquid inlet;
the hydrogen sulfide gas outlet of the desorption tower is connected to the hydrogen sulfide inlet on the upper portion of the cold trap, the hydrogen sulfide gas outlet is further arranged on the upper portion of the cold trap and connected to the compressor, the absorbent barren solution outlet is arranged at the bottom of the cold trap and connected to the reflux port of the desorption tower, and the low-temperature water outlet and the low-temperature water inlet are respectively arranged on the upper portion and the lower portion of the side wall of the cold trap.
According to a further scheme, the absorption tower adopts an assembled packing absorption tower and is divided into a tower top section, a tower bottom section and a tower middle section, the tower height is adjusted in an increasing and decreasing mode through the tower middle section according to absorption requirements, each tower section is provided with a pressure monitoring meter, and the tower top and a tower kettle are respectively provided with a temperature monitoring meter.
According to a further scheme, the analysis tower adopts a plate analysis tower provided with an absorption reboiler, the analysis tower adopts an assembled plate analysis tower and is divided into a tower top section, a tower bottom section and a tower middle section, the tower height is adjusted in an increasing and decreasing mode through the tower middle section according to absorption requirements, each tower section is provided with a pressure monitoring meter, and the tower top and the tower kettle are respectively provided with a temperature monitoring meter. The siphon reboiler can be dismantled, changes different specification reboilers according to the reboiling demand.
Further scheme, this system still includes industrial gas moisture removal fluid reservoir, and the setting of knockout drum is the double-deck jar of clamp cover, leads to the refrigerant in the clamp cover, and jar body temperature keeps within 5 ℃, and jar internal liquid baffle, demister and the hydrops package of setting up, and the liquid of condensation collects the back and discharges in the hydrops package, and gas gets into the absorption tower through the demister.
According to a further scheme, the system further comprises an automatic control system, the analysis temperature is too high, energy is wasted, the absorbent is possibly damaged, and the analysis temperature is too low to be completely analyzed. The temperature of the hydrogen sulfide gas after the desorption in the desorption tower controls the ventilation of the steam inlet of the reboiler, so that the desorption temperature is suitable.
The utility model discloses specifically use the step as follows:
the method comprises the following steps: the industrial gas containing hydrogen sulfide and an absorbent enter a liquid separation tank to remove water and hydrocarbon substances, and the purified industrial gas enters the next step for treatment;
step two: the industrial gas containing hydrogen sulfide and an absorbent enter an absorption tower, a chemical reaction is carried out in the absorption tower to generate purified gas and absorbent rich liquid containing the hydrogen sulfide absorbent, the purified gas is discharged out of the absorption tower, and the absorbent rich liquid enters the next step for treatment;
step three: pumping the absorbent rich solution into a lean rich solution heat exchanger through an absorbent rich solution pump for heat exchange, then feeding the absorbent rich solution into an analytical tower, and desorbing hydrogen sulfide and a clean absorbent, namely absorbent lean solution, under the conditions of heating and pressure reduction;
step IV: through desorption, the absorbent barren solution is pumped into the barren and rich solution heat exchanger through an absorbent barren solution pump to exchange heat and then returns to the absorption tower for recycling;
step five: and thirdly, discharging the desorbed hydrogen sulfide after the treatment of the cold trap, wherein the final purity of the hydrogen sulfide can reach more than 99%, and discharging the hydrogen sulfide gas to enter a factory for recycling through a compressor.
The utility model discloses an effect and advantage are: the hydrogen sulfide gas in the industrial gas can be recovered with high selectivity, and continuous production can be realized by absorption and analysis; the difference of the hydrogen sulfide content of the tail gas after absorption can be realized through the difference of the absorption stages; the raw material absorbent has extremely low loss, the annual loss rate is 1-2%, and the operation cost is low. Compared with the existing industrial tail gas treatment technology, the method can greatly reduce the operation cost, greatly improve the absorption efficiency of the hydrogen sulfide, does not produce secondary pollution, has high purity of the recovered hydrogen sulfide, and can recycle the hydrogen sulfide gas and change waste into valuable.
Drawings
FIG. 1 is a schematic view of a process system of the present invention;
reference numerals:
1-liquid separation tank, 2-absorption tower, 3-absorbent pregnant solution pump, 4-lean pregnant solution heat exchanger, 5-absorbent pregnant solution pump, 6-desorption tower, 7-siphon reboiler, 8-cold trap, 9-compressor
CWS: circulating the water on the water; CWR: returning circulating water; LS: low-pressure saturated steam; SC: steam condensate water; LWS: low-temperature water is added; LWR: and returning low-temperature water.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Example 1
As shown in fig. 1, a system for recovering hydrogen sulfide gas with high selectivity comprises a liquid separation tank 1, an absorption tower 2, an absorbent rich liquid pump 3, a lean rich liquid heat exchanger 4, an absorbent lean liquid pump 5, a desorption tower 6, a siphon reboiler 7, a cold trap 8 and a compressor 9;
the liquid separation tank 1 is a jacket double-layer tank, a refrigerant is introduced into the jacket, the temperature of the tank body is kept within 5 ℃, a liquid baffle plate, a demister and a liquid accumulation bag are arranged in the tank body, condensed liquid is collected in the liquid accumulation bag and then discharged, and gas enters the absorption tower 2 through the demister;
the lower part of the absorption tower 2 is provided with a gas inlet to be recovered, the upper part of the absorption tower is provided with an absorbent inlet and a purified gas outlet, the bottom of the absorption tower is provided with an absorbent rich liquid outlet, and the absorbent rich liquid outlet is connected to an absorbent rich liquid pump 3;
the upper part of the desorption tower 6 is provided with an absorbent rich liquid inlet and a sulfuration hydrogenolysis gas-evolution outlet, the lower part is connected with a siphon reboiler 7, and the bottom is provided with an absorbent lean liquid outlet; the absorbent lean liquid outlet is connected to an absorbent lean liquid pump 5;
the absorption agent rich liquid pump 3 and the absorption agent barren liquid pump 5 pump out feed liquid and respectively enter a barren and rich liquid heat exchanger 4, after heat exchange, the absorption agent barren liquid is connected to an absorption agent barren liquid inlet arranged at the upper part of the absorption tower, and the absorption agent rich liquid is connected to an absorption agent rich liquid inlet arranged at the upper part of the desorption tower;
the hydrogen sulfide gas outlet of the desorption tower 6 is connected to the hydrogen sulfide inlet on the upper portion of the cold trap 8, the hydrogen sulfide gas outlet on the upper portion of the cold trap 8 is connected to the compressor 9, the absorbent barren solution outlet is arranged at the bottom of the cold trap and connected to the reflux port of the desorption tower 6, and the upper portion and the lower portion of the side wall of the cold trap 8 are respectively provided with a low-temperature water outlet and a low-temperature water inlet.
Example 2
The system of the embodiment 1 is adopted to treat the mixed industrial gas of hydrogen sulfide and carbon dioxide, wherein the content of hydrogen sulfide is 5 percent and the content of carbon dioxide is 95 percent, and the specific steps are as follows:
the method comprises the following steps: the industrial gas containing hydrogen sulfide and an absorbent enter a liquid separation tank to remove water and hydrocarbon substances, and the purified industrial gas enters the next step for treatment;
step two: the industrial gas containing hydrogen sulfide and an absorbent enter an absorption tower, a chemical reaction is carried out in the absorption tower to generate purified gas and absorbent rich liquid containing the hydrogen sulfide absorbent, the purified gas is discharged out of the absorption tower, and the absorbent rich liquid enters the next step for treatment;
step three: pumping the absorbent rich solution into a lean rich solution heat exchanger through an absorbent rich solution pump for heat exchange, then feeding the absorbent rich solution into an analytical tower, and desorbing hydrogen sulfide and a clean absorbent, namely absorbent lean solution, under the conditions of heating and pressure reduction;
step IV: through desorption, the absorbent barren solution is pumped into the barren and rich solution heat exchanger through an absorbent barren solution pump to exchange heat and then returns to the absorption tower for recycling;
step five: and thirdly, discharging the desorbed hydrogen sulfide after the treatment of the cold trap, wherein the final purity of the hydrogen sulfide can reach more than 99%, and discharging the hydrogen sulfide gas to enter a factory for recycling through a compressor.
Strong alkaline proton type ionic liquid is used as an absorbent, the parameters of an absorption tower are phi 800 multiplied by 4000, the absorption pressure is 0.1Mpa, the absorption temperature is 60 ℃, the absorption amount is 2.5mol/kg, the parameters of an analytical tower are phi 800 multiplied by 4000, the analytical pressure is 0.01Mpa, and the analytical temperature is 100 ℃. After absorption, the hydrogen sulfide content was discharged in an amount of 99%.
Although the preferred embodiments of the present patent have been described in detail, the present patent is not limited to the above embodiments, and various changes can be made without departing from the spirit of the present patent within the knowledge of those skilled in the art.
Claims (8)
1. A system for recovering hydrogen sulfide gas with high selectivity is characterized in that: the system comprises a liquid separation tank (1), an absorption tower (2), an absorbent pregnant solution pump (3), a lean pregnant solution heat exchanger (4), an absorbent lean solution pump (5), a desorption tower (6), a siphon reboiler (7), a cold trap (8) and a compressor (9);
the liquid separation tank (1) is arranged into a jacket double-layer tank, a refrigerant is introduced into the jacket, the temperature of the tank body is kept within 5 ℃, a liquid baffle plate, a demister and a liquid accumulation bag are arranged in the tank body, condensed liquid is collected in the liquid accumulation bag and then discharged, and gas enters the absorption tower (2) through the demister;
the lower part of the absorption tower (2) is provided with a gas inlet to be recovered, the upper part of the absorption tower is provided with an absorbent inlet and a purified gas outlet, the bottom of the absorption tower is provided with an absorbent rich liquid outlet, and the absorbent rich liquid outlet is connected to an absorbent rich liquid pump (3);
the upper part of the desorption tower (6) is provided with an absorbent rich liquid inlet and a sulfuration hydrogenolysis gas evolution outlet, the lower part of the desorption tower is connected with a siphon reboiler (7), and the bottom of the desorption tower is provided with an absorbent lean liquid outlet; the absorbent lean liquid outlet is connected to an absorbent lean liquid pump (5);
the absorption agent rich liquid pump (3) and the absorption agent lean liquid pump (5) pump out feed liquid and respectively enter the lean and rich liquid heat exchanger (4), after heat exchange, the absorption agent lean liquid is connected to an absorption agent lean liquid inlet arranged at the upper part of the absorption tower (2), and the absorption agent rich liquid is connected to an absorption agent rich liquid inlet arranged at the upper part of the desorption tower (6);
the hydrogen sulfide gas outlet of the desorption tower (6) is connected to the hydrogen sulfide inlet on the upper portion of the cold trap (8), the upper portion of the cold trap (8) is further provided with a hydrogen sulfide gas outlet connected to the compressor (9), the bottom of the cold trap (8) is provided with an absorbent barren liquor outlet and is connected to the reflux port of the desorption tower (6), and the upper portion and the lower portion of the side wall of the cold trap (8) are respectively provided with a low-temperature water outlet and a low-temperature water inlet.
2. The system for recovering hydrogen sulfide gas with high selectivity according to claim 1, wherein: the absorption tower adopts a filler absorption tower.
3. The system for recovering hydrogen sulfide gas with high selectivity according to claim 2, wherein: the absorption tower is divided into a tower top section, a tower bottom section and a tower middle section, the tower height is adjusted in an increasing and decreasing mode through the tower middle section according to absorption requirements, each tower section is provided with a pressure monitoring meter, and the tower top and the tower kettle are respectively provided with a temperature monitoring meter.
4. The system for recovering hydrogen sulfide gas with high selectivity according to claim 2, wherein: the desorption tower adopts a plate-type desorption tower provided with an absorption reboiler.
5. The system for recovering hydrogen sulfide gas with high selectivity according to claim 4, wherein: the analysis tower adopts an assembled plate analysis tower, and is divided into a tower top section, a tower bottom section and a tower middle section, the tower height is increased and decreased through the tower middle section according to the absorption requirement, each tower section is provided with a pressure monitoring meter, and the tower top and the tower kettle are respectively provided with a temperature monitoring meter.
6. The system for recovering hydrogen sulfide gas with high selectivity according to claim 1, wherein: the siphon reboiler can be dismantled, and different specification reboilers are changed according to the reboiling demand.
7. The system for recovering hydrogen sulfide gas with high selectivity according to claim 1, wherein: the system further comprises an industrial gas moisture removal liquid tank, the liquid separation tank is a jacket double-layer tank, a refrigerant is introduced into the jacket, the temperature of the tank body is kept within 5 ℃, a liquid baffle plate, a demister and a liquid accumulation bag are arranged in the tank body, condensed liquid is collected in the liquid accumulation bag and then discharged, and gas enters the absorption tower through the demister.
8. The system for recovering hydrogen sulfide gas with high selectivity according to claim 1, wherein: the system also comprises an automatic control system, the analysis temperature is too high, energy is wasted and the absorbent is possibly damaged, the analysis temperature is too low and cannot be completely analyzed, and the temperature of the hydrogen sulfide gas after analysis by the analysis tower controls the ventilation of the steam inlet of the reboiler to ensure that the analysis temperature is suitable.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202022615114.0U CN213610621U (en) | 2020-11-12 | 2020-11-12 | System for hydrogen sulfide gas is retrieved to high selectivity |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202022615114.0U CN213610621U (en) | 2020-11-12 | 2020-11-12 | System for hydrogen sulfide gas is retrieved to high selectivity |
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