CN219239265U - Hydrogenation tail gas entrained working solution recovery system - Google Patents
Hydrogenation tail gas entrained working solution recovery system Download PDFInfo
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- CN219239265U CN219239265U CN202320735587.5U CN202320735587U CN219239265U CN 219239265 U CN219239265 U CN 219239265U CN 202320735587 U CN202320735587 U CN 202320735587U CN 219239265 U CN219239265 U CN 219239265U
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Abstract
The utility model discloses a hydrogenation tail gas entrained working solution recovery system, which comprises a hydrogenation tower; the tail gas condensate receiving tank is communicated with the air inlet of the torch emptying separation tank, and the tail gas outlet of the torch emptying separation tank is connected to the torch system; the bottom liquid outlet of the torch emptying separation tank is communicated with the inlet of the preparation kettle; the preparation kettle is communicated with an inlet of a working solution high-level tank, the working solution high-level tank is communicated with an alkali separator, an outlet of the alkali separator is communicated with a clay bed, a liquid outlet of the clay bed is communicated with a regenerated solution storage tank, and the regenerated solution storage tank is communicated with a hydrogenation tower. The advantages are that: and after the gas which is not fully reacted in the hydrogenation tower is condensed by the tail gas emptying condenser, the gas phase is discharged from the top of the tail gas condensate receiving tank to enter the torch emptying separation tank, the working solution carried by the gas phase is further condensed and separated, the separated working solution is recycled to the preparation kettle, the working solution carried in the tail gas is effectively recycled, and the treated tail gas is discharged from the fire removing torch system, so that the potential safety hazard is reduced.
Description
Technical field:
the utility model relates to the technical field of hydrogen peroxide production, in particular to a hydrogenation tail gas entrained working solution recovery system.
The background technology is as follows:
in the production process of hydrogen peroxide by anthraquinone method, in the hydrogenation process, working solution from post-treatment process mainly comprises heavy aromatic hydrocarbon and trioctyl phosphate which are mixed according to a certain proportion as solvent and 2-ethyl anthraquinone as solute, wherein the temperature of the working solution and hydrogen provided by a hydrogen production workshop are controlled within 40-55 ℃ in a hydrogenation tower, the pressure is controlled within 0.18-0.35MPa, and hydrogenation reaction is carried out to generate hydroanthraquinone and byproducts; and after the hydrogen and the inert gas (nitrogen) which do not completely participate in the reaction are condensed by a tail gas emptying condenser, the hydrogen and the inert gas are directly emptied, and the condensate is recycled to a tail gas condensate receiving tank.
The existing problems are that only part of working solution entrained by gas phase phenomenon can be condensed by a tail gas emptying condenser to enter a tail gas condensate receiving tank, and the working solution is not completely recovered, so that economic loss is caused; in addition, the direct emptying of the tail gas can cause the exceeding of non-methane total hydrocarbon, and meanwhile, hydrogen in the tail gas is easy to catch fire and explode when meeting static sparks, so that unsafe hidden danger exists.
The utility model comprises the following steps:
the utility model aims to provide a hydrogenated tail gas entrainment working solution recovery system which can effectively recover tail gas working solution to reduce economic loss.
The utility model is implemented by the following technical scheme: a hydrogenation tail gas entrained working solution recovery system comprises a hydrogenation tower, a tail gas emptying condenser, a tail gas condensate receiving tank, a torch emptying separation tank, a preparation kettle and a working solution overhead tank; the tail gas vent of the hydrogenation tower is communicated with the gas inlet of the tail gas vent condenser, the outlet of the tail gas vent condenser is communicated with the inlet of the tail gas condensate receiving tank, the top gas outlet of the tail gas condensate receiving tank is communicated with the gas inlet of the torch vent separation tank, and the tail gas outlet of the torch vent separation tank is connected to a torch system; the bottom liquid outlet of the tail gas condensate receiving tank is communicated with the inlet of the alkaline recovery tank, the outlet of the alkaline recovery tank is communicated with the inlet of the preparation kettle through a pump, and the bottom liquid outlet of the torch emptying separation tank is communicated with the inlet of the preparation kettle; the liquid outlet of the preparation kettle is communicated with the inlet of the working liquid high-level tank through a pump, the outlet of the working liquid high-level tank is communicated with the inlet of the alkali separator, the outlet of the alkali separator is communicated with the clay bed, the liquid outlet of the clay bed is communicated with the regenerated liquid storage tank, and the outlet of the regenerated liquid storage tank is communicated with the liquid inlet of the hydrogenation tower through a pump.
Further, a check valve and a flame arrester are arranged on the tail gas pipeline of the torch emptying separation tank.
Further, the hydrogenated liquid outlet of the hydrogenation tower is communicated with the hydrogenated liquid storage tank, the hydrogenated liquid storage tank is communicated with the liquid inlet of the oxidation tower through a pump, the oxidized liquid outlet of the oxidation tower is communicated with the oxidized liquid storage tank, the oxidized liquid storage tank is communicated with the extraction tower through a pump, the raffinate outlet of the extraction tower is communicated with the inlet of the alkali tower, the outlet of the alkali tower is communicated with the inlet of the alkali separator, and the extract outlet of the extraction tower is communicated with the purification tower.
The utility model has the advantages that: the hydrogen gas which is not fully reacted in the hydrogenation tower and inert gas released from the liquid phase are condensed by the tail gas emptying condenser, part of condensed working solution enters the tail gas condensate receiving tank and is then discharged to the alkaline recovery tank for recovery, the alkaline recovery tank is pumped to be used for cleaning, the gas phase is discharged from the top of the tail gas condensate receiving tank and enters the torch emptying separation tank, the working solution entrained in the gas phase is further condensed and separated, the separated working solution is recovered to the preparation tank, the working solution entrained in the tail gas is effectively recovered, and the treated tail gas passes through the check valve and the flame arrester and then is closely discharged to the fire torch system, so that the potential safety hazard is reduced.
Description of the drawings:
fig. 1 is a schematic structural view of the present utility model.
The components in the drawings are marked as follows: the hydrogenation tower 1, a tail gas emptying condenser 2, a tail gas condensate receiving tank 3, a torch emptying separation tank 4, a preparation kettle 5, a working solution overhead tank 6, a torch system 7, an alkaline recovery tank 8, an alkaline separator 9, a clay bed 10, a regenerated solution storage tank 11, a check valve 12, a flame arrester 13, a hydrogenated solution storage tank 14, an oxidation tower 15, an oxidation solution storage tank 16, an extraction tower 17, an alkaline tower 18 and a purification tower 19.
The specific embodiment is as follows:
the following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
As shown in fig. 1, the embodiment provides a hydrogenation tail gas entrainment working solution recovery system, which comprises a hydrogenation tower 1, a tail gas emptying condenser 2, a tail gas condensate receiving tank 3, a torch emptying separation tank 4, a preparation kettle 5 and a working solution overhead tank 6.
The hydrogenation tower 1 is communicated with a hydrogen pipeline, the oxidation tower 15 is communicated with a compressed air pipeline, the hydrogenation liquid outlet of the hydrogenation tower 1 is communicated with the hydrogenation liquid storage tank 14, the hydrogenation liquid storage tank 14 is communicated with the liquid inlet of the oxidation tower 15 through a pump, the oxidation liquid outlet of the oxidation tower 15 is communicated with the oxidation liquid storage tank 16, the oxidation liquid storage tank 16 is communicated with the extraction tower 17 through a pump, the raffinate outlet of the extraction tower 17 is communicated with the inlet of the alkali tower 18, the outlet of the alkali tower 18 is communicated with the inlet of the alkali separator 9, and the extract outlet of the extraction tower 17 is communicated with the purification tower 19.
The hydrogen and the working solution are subjected to hydrogenation reaction in the hydrogenation tower 1, the reacted hydrogenation solution enters a hydrogenation solution storage tank 14, is pumped into an oxidation tower 15, and flows upwards together with clean air entering the bottom of the tower to further perform oxidation reaction; the oxidation liquid discharged from the oxidation tower 15 enters an oxidation liquid storage tank 16 and is pumped into an extraction tower 17, namely, the oxidation liquid containing hydrogen peroxide enters from the feeding end at the bottom of the extraction tower 17, after being treated by the extraction tower 17, the extraction liquid or crude hydrogen peroxide flows out from the discharging end at the bottom of the tower and enters the feeding end at the top of a purification tower 19, the raffinate flowing out from the top of the tower enters an alkali tower 18 for alkali washing, and then is discharged into an alkali separator 9, so that possible entrained potassium carbonate solution drops are separated, and then enters the bottom of the clay bed 10 through the level difference.
The tail gas emptying port of the hydrogenation tower 1 is communicated with the air inlet of the tail gas emptying condenser 2, the outlet of the tail gas emptying condenser 2 is communicated with the inlet of the tail gas condensate receiving tank 3, the top air outlet of the tail gas condensate receiving tank 3 is communicated with the air inlet of the torch emptying separation tank 4, the tail gas outlet of the torch emptying separation tank 4 is connected to the torch system 7, and the torch emptying separation tank 4 is an existing gas-liquid separation tank; the bottom liquid outlet of the tail gas condensate receiving tank 3 is communicated with the inlet of the alkaline recovery tank 8, the outlet of the alkaline recovery tank 8 is communicated with the inlet of the preparation kettle 5 through a pump, and the bottom liquid outlet of the torch emptying separation tank 4 is communicated with the inlet of the preparation kettle 5; the preparation kettle 5 is mainly used for preparing the original starting fresh working solution; and (3) during the production process, the old working solution in the system is withdrawn and cleaned, degradation products generated during the production process are removed, and the recovered working solution is cleaned again.
A check valve 12 and a flame arrester 13 are arranged on a tail gas pipeline of the torch emptying separation tank 4, a liquid outlet of the preparation kettle 5 is communicated with an inlet of the working liquid high-level tank 6 through a pump, an outlet of the working liquid high-level tank 6 is communicated with an inlet of the alkali separator 9, an outlet of the alkali separator 9 is communicated with the clay bed 10, a liquid outlet of the clay bed 10 is communicated with a regenerated liquid storage tank 11, and an outlet of the regenerated liquid storage tank 11 is communicated with a liquid inlet of the hydrogenation tower 1 through a pump; the hydrogen gas which is not fully reacted in the hydrogenation tower 1 and inert gas released from the liquid phase are condensed by the tail gas emptying condenser 2, the partially condensed working solution enters the tail gas condensate receiving tank 3 and is discharged to the alkaline recovery tank 8 for recovery, the alkaline recovery tank is pumped to the preparation kettle 5 for cleaning, the gas phase comes out from the top of the tail gas condensate receiving tank 3 and enters the torch emptying separation tank 4, the working solution carried by the gas phase is further condensed and separated, the separated working solution is recovered to the preparation kettle 5, the working solution carried by the tail gas is effectively recovered, and the treated tail gas passes through the check valve 12 and the flame arrester 13 and is then discharged in a closed manner to the fire-removing torch system 7, so that the potential safety hazard is reduced.
The working solution in the preparation kettle 5 is pumped into the working solution overhead tank 6 and mixed with the working solution from the alkali tower 18 to enter the clay bed 10, and activated alumina is filled in the clay bed 10 and used for regenerating anthraquinone degradation products possibly generated in the reaction process and adsorbing potassium carbonate liquid drops in the working solution, and the working solution flowing out of the clay bed 10 enters the regenerated solution storage tank 11 and is pumped into the hydrogenation tower 1 by a pump to continuously participate in hydrogenation reaction; the working solution is effectively recycled, the cost is saved, and the economic loss is reduced.
The foregoing description of the preferred embodiments of the utility model is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the utility model.
Claims (3)
1. The hydrogenation tail gas entrained working solution recycling system is characterized by comprising a hydrogenation tower, a tail gas emptying condenser, a tail gas condensate receiving tank, a torch emptying separation tank, a preparation kettle and a working solution overhead tank;
the tail gas vent of the hydrogenation tower is communicated with the gas inlet of the tail gas vent condenser, the outlet of the tail gas vent condenser is communicated with the inlet of the tail gas condensate receiving tank, the top gas outlet of the tail gas condensate receiving tank is communicated with the gas inlet of the torch vent separation tank, and the tail gas outlet of the torch vent separation tank is connected to a torch system;
the bottom liquid outlet of the tail gas condensate receiving tank is communicated with the inlet of the alkaline recovery tank, the outlet of the alkaline recovery tank is communicated with the inlet of the preparation kettle through a pump, and the bottom liquid outlet of the torch emptying separation tank is communicated with the inlet of the preparation kettle;
the liquid outlet of the preparation kettle is communicated with the inlet of the working liquid high-level tank through a pump, the outlet of the working liquid high-level tank is communicated with the inlet of the alkali separator, the outlet of the alkali separator is communicated with the clay bed, the liquid outlet of the clay bed is communicated with the regenerated liquid storage tank, and the outlet of the regenerated liquid storage tank is communicated with the liquid inlet of the hydrogenation tower through a pump.
2. The hydrogenated tail gas entrained working fluid recovery system according to claim 1, wherein a check valve and a flame arrester are installed on a tail gas pipeline of the flare blow-down separation tank.
3. The system of claim 1, wherein the hydrogenation liquid outlet of the hydrogenation tower is connected to a hydrogenation liquid storage tank, the hydrogenation liquid storage tank is connected to a liquid inlet of an oxidation tower by a pump, the oxidation liquid outlet of the oxidation tower is connected to an oxidation liquid storage tank, the oxidation liquid storage tank is connected to an extraction tower by a pump, a raffinate outlet of the extraction tower is connected to an inlet of a base tower, an outlet of the base tower is connected to an inlet of the base separator, and an extract outlet of the extraction tower is connected to a purification tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320735587.5U CN219239265U (en) | 2023-04-04 | 2023-04-04 | Hydrogenation tail gas entrained working solution recovery system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320735587.5U CN219239265U (en) | 2023-04-04 | 2023-04-04 | Hydrogenation tail gas entrained working solution recovery system |
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| Publication Number | Publication Date |
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| CN219239265U true CN219239265U (en) | 2023-06-23 |
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| CN202320735587.5U Active CN219239265U (en) | 2023-04-04 | 2023-04-04 | Hydrogenation tail gas entrained working solution recovery system |
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- 2023-04-04 CN CN202320735587.5U patent/CN219239265U/en active Active
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