CN212560125U - Novel coke oven gas desulfurization system - Google Patents
Novel coke oven gas desulfurization system Download PDFInfo
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- CN212560125U CN212560125U CN202021295817.3U CN202021295817U CN212560125U CN 212560125 U CN212560125 U CN 212560125U CN 202021295817 U CN202021295817 U CN 202021295817U CN 212560125 U CN212560125 U CN 212560125U
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Abstract
The utility model relates to a coke oven gas desulfurization technical field specifically discloses a novel coke oven gas desulfurization system, including absorption tower and regenerator, the bottom intercommunication of absorption tower has rich liquid pump, and rich liquid pump's output intercommunication has the rich liquid filter, and regenerator's bottom intercommunication has lean rich liquid heat exchanger, and rich liquid filter communicates with lean rich liquid heat exchanger, an output of lean rich liquid heat exchanger with regenerator's upper portion intercommunication, another output intercommunication of lean rich liquid heat exchanger has the lean solution groove, and lean solution groove's exit end communicates with absorber's upper portion through the lean liquid pump, and regenerator's lower part and reboiler form circulation circuit, and regenerator's top intercommunication has vapor compressor, vapor compressor with reboiler intercommunication, another output intercommunication of reboiler has acid gas separator, acid gas separator passes through the backwash pump and regenerator's upper portion intercommunication, the utility model discloses a heat pump technique can save low pressure steam consumption, and simple process energy consumption is low.
Description
Technical Field
The utility model relates to a coke oven gas desulfurization technical field especially relates to a novel coke oven gas desulfurization system.
Background
At present, the main domestic coke oven gas wet desulphurization methods are a wet oxidation method and a chemical method, the wet oxidation method comprises a tannin extract method, an HPF method, an FRC method and the like, and the chemical absorption method mainly comprises vacuum potassium carbonate and the like.
The tannin extract method is independently developed by China and is one of the more domestic desulfurization methods at present. The principle is that tannin extract is used as a main catalyst, alkaline oxidation degradation products of the tannin extract are used as an intermediate oxygen carrier in a wet-type binary oxidation desulfurization method, the alkaline oxidation degradation products of the tannin extract are used as a complexing agent of vanadium and are mixed with alkali vanadium to prepare an aqueous solution, gaseous hydrogen sulfide is absorbed and converted into elemental sulfur, but the solution absorbs CO2Therefore, the pH value of the solution is lowered, which affects the desulfurization efficiency and lowers the desulfurization accuracy. In addition, the equipment using the tannin extract desulfurization method is large, the gas amount which can be treated is small, and the purity of sulfur obtained after desulfurization is not high, thus being not beneficial to processing.
The HPF desulfurization process takes ammonia in coal gas as an alkali source, and the desulfurization solution is oxidized and regenerated under the action of the composite catalyst HPF after absorbing hydrogen sulfide in the coal gas, so that the hydrogen sulfide is finally converted into elemental sulfur to be removed, and the desulfurization solution is recycled.
The FRC method is developed by Japan and is to remove H from coke oven gas by ammonia in the presence of picric acid as catalyst2S, removing HCN by using ammonium polysulfide, but the use of the picric acid is limited to a certain extent due to the factors of difficult transportation and storage, long process flow, large occupied area, large investment and the like because the picric acid is an explosion dangerous article.
The vacuum sodium carbonate method is to desulfurize by Na2CO3H in the gas is removed in an absorption tower as alkali liquor2S and HCN, purifying the coal gas, and then sending the solution containing NaHS after the reaction into a regeneration tower to resolve H2Acid gases such as S and HCN, Na2CO3The solution is recycled, and the method is used for desulfurizationLow efficiency, outlet H2And S does not reach the standard.
Both wet oxidation and chemical absorption methods have problems of poor capability of removing organic sulfur and low desulfurization accuracy, and a certain amount of waste liquid is generated with increase of products of side reactions and other impurities in the solution, and the treatment of the waste liquid is also a problem.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems mentioned in the background art, the utility model aims to provide a novel coke oven gas desulfurization system.
In order to realize the above object, the technical scheme of the utility model is that:
a novel coke oven gas desulfurization system comprises an absorption tower and a regeneration tower, wherein the top of the absorption tower is communicated with a purifier separator, the lower part of the absorption tower is communicated with a raw material gas separator, the bottom of the absorption tower is communicated with a pregnant solution pump, the output end of the pregnant solution pump is communicated with a pregnant solution filter, the bottom of the regeneration tower is communicated with a poor pregnant solution heat exchanger, the pregnant solution filter is communicated with the poor pregnant solution heat exchanger, one output end of the poor pregnant solution heat exchanger is communicated with the upper part of the regeneration tower, the other output end of the poor pregnant solution heat exchanger is communicated with a poor solution tank, the outlet end of the poor solution tank is communicated with a poor solution pump, the output end of a reboiler is communicated with the upper part of the absorption tower, the lower part of the regeneration tower is communicated with a reboiler, and one output end of the reboiler forms a circulation loop with the regeneration tower through a pipeline, the top of the regeneration tower is communicated with a steam compressor, the steam compressor is communicated with the reboiler, the other output end of the reboiler is communicated with an acid gas separator, the bottom of the acid gas separator is communicated with a reflux pump, and the output end of the reflux pump is communicated with the upper part of the regeneration tower.
Furthermore, a lean liquid filter is communicated between the lean liquid pump and the absorption tower, and a lean liquid cooler is communicated between the lean liquid filter and the lean liquid pump.
Further, a pressure reducing valve is communicated between the reboiler and the acid gas separator, and an acid gas cooler is communicated between the pressure reducing valve and the acid gas separator.
The utility model has the advantages that: the utility model discloses a heat pump technique, the latent heat of recycle regenerator column overhead gas utilizes the heat source of the reboiler at the regenerator column bottom behind the vapor compressor with acid gas pressurization, can save low pressure steam consumption, and simple process energy consumption is low.
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Fig. 1 is a schematic structural view of the present invention;
description of the figure numbering: 1. the system comprises an absorption tower, 2, a rich liquid pump, 3, a rich liquid filter, 4, a lean and rich liquid heat exchanger, 5, a regeneration tower, 6, a reboiler, 7, an acid gas cooler, 8, an acid gas separator, 9, a reflux pump, 10, a lean liquid tank, 11, a lean liquid pump, 12, a lean liquid cooler, 13, a lean liquid filter, 14, a raw material gas separator, 15, a purification gas separator, 16, a vapor compressor, 17 and a pressure reducing valve.
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. All other embodiments obtained by a person skilled in the art based on the embodiments of the present invention belong to the protection scope of the present invention.
As shown in figure 1, a novel coke oven gas desulfurization system comprises an absorption tower and a regeneration tower, wherein the top of the absorption tower is communicated with a purifier separator, the lower part of the absorption tower is communicated with a raw material gas separator, the bottom of the absorption tower is communicated with a pregnant solution pump, the output end of the pregnant solution pump is communicated with a pregnant solution filter, the bottom of the regeneration tower is communicated with a poor pregnant solution heat exchanger, the pregnant solution filter is communicated with the poor pregnant solution heat exchanger, one output end of the poor pregnant solution heat exchanger is communicated with the upper part of the regeneration tower, the other output end of the poor pregnant solution heat exchanger is communicated with a poor solution tank, the outlet end of the poor solution tank is communicated with a poor solution pump, the output end of the poor solution pump is communicated with the upper part of the absorption tower, the lower part of the regeneration tower is communicated with a reboiler, one output end of the reboiler forms a tower-shaped circulation loop with the regeneration tower, the other output end of the reboiler is communicated with an acid gas separator, the bottom of the acid gas separator is communicated with a reflux pump, and the output end of the reflux pump is communicated with the upper part of the regeneration tower.
In the actual desulfurization process, the method comprises the following steps:
s1: after the coke oven gas from the outside is separated from liquid by the raw material gas separator, the gas from bottom to top passes through the absorption tower to be fully contacted with the desulfurizing agent flowing reversely from top to bottom in the absorption tower, and H in the gas2S acid gas is absorbed and enters a liquid phase, and the total sulfur in the purified gas is removed to 20mg/Nm3Then, the mixture is removed outside after passing through a purifier separator;
s2: absorb H2After the rich solution of S is boosted by a rich solution pump, filtering trace impurities in the solution in a rich solution filter, exchanging heat with the lean solution flowing out of the bottom of the regeneration tower through a lean rich solution heat exchanger, raising the temperature, and then feeding the lean solution to the upper part of the regeneration tower, wherein the rich solution is fully contacted with reversely flowing steam from top to bottom through the regeneration tower to fully contact H in the rich solution2S acid gas is resolved, and H is separated by a steam compressor2S acid gas is pressurized to 4bar.g and then is used as a heat source of a reboiler at the bottom of the regeneration tower, condensate enters an acid gas separator after being decompressed and cooled, separated liquid returns to the regeneration tower, and H2S acid gas Sulfur recovery Unit, H2The concentration of S is 80%;
s3: the barren liquor regenerated at the bottom of the regeneration tower enters a barren liquor tank after heat exchange and temperature reduction, the barren liquor is pressurized by a barren liquor pump and then is sent back to the absorption tower for recycling, and low-pressure steam and H at the top of the regeneration tower are utilized2The S acid gas provides a heat source for the regeneration tower.
In the embodiment, a lean solution filter is communicated between the lean solution pump and the absorption tower, the lean solution filter is arranged to filter part of the solution on line, a lean solution cooler is communicated between the lean solution filter and the lean solution pump, and the lean solution cooler is arranged to cool the lean solution.
In this embodiment, a pressure reducing valve is communicated between the reboiler and the acid gas separator to reduce the pressure of the acid gas, and an acid gas cooler is communicated between the pressure reducing valve and the acid gas separator to reduce the temperature of the acid gas.
The utility model discloses a heat pump technique, the latent heat of recycle regenerator column overhead gas utilizes the heat source of the reboiler at the regenerator column bottom behind the vapor compressor with acid gas pressurization, can save low pressure steam consumption, and simple process energy consumption is low.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not intended to limit the present invention, and all modifications, equivalents, improvements and the like that are within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (3)
1. A novel coke oven gas desulfurization system is characterized by comprising an absorption tower and a regeneration tower, wherein the top of the absorption tower is communicated with a purifier separator, the lower part of the absorption tower is communicated with a raw material gas separator, the bottom of the absorption tower is communicated with a pregnant solution pump, the output end of the pregnant solution pump is communicated with a pregnant solution filter, the bottom of the regeneration tower is communicated with a lean and pregnant solution heat exchanger, the pregnant solution filter is communicated with the lean and pregnant solution heat exchanger, one output end of the lean and pregnant solution heat exchanger is communicated with the upper part of the regeneration tower, the other output end of the lean and pregnant solution heat exchanger is communicated with a lean solution tank, the outlet end of the lean solution tank is communicated with a lean solution pump, the output end of the lean solution pump is communicated with the upper part of the absorption tower, the lower part of the regeneration tower is communicated with a reboiler, and one output end of the reboiler forms a circulation loop with the regeneration tower, the top of the regeneration tower is communicated with a steam compressor, the steam compressor is communicated with the reboiler, the other output end of the reboiler is communicated with an acid gas separator, the bottom of the acid gas separator is communicated with a reflux pump, and the output end of the reflux pump is communicated with the upper part of the regeneration tower.
2. The novel coke oven gas desulfurization system of claim 1, wherein a barren liquor filter is communicated between the barren liquor pump and the absorption tower, and a barren liquor cooler is communicated between the barren liquor filter and the barren liquor pump.
3. The novel coke oven gas desulfurization system of claim 1, wherein a pressure reducing valve is communicated between the reboiler and the acid gas separator, and an acid gas cooler is communicated between the pressure reducing valve and the acid gas separator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021295817.3U CN212560125U (en) | 2020-07-03 | 2020-07-03 | Novel coke oven gas desulfurization system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021295817.3U CN212560125U (en) | 2020-07-03 | 2020-07-03 | Novel coke oven gas desulfurization system |
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| CN212560125U true CN212560125U (en) | 2021-02-19 |
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| CN202021295817.3U Active CN212560125U (en) | 2020-07-03 | 2020-07-03 | Novel coke oven gas desulfurization system |
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