CN211635902U - Separation system of hydrogen chloride and sulfur dioxide gas mixture - Google Patents
Separation system of hydrogen chloride and sulfur dioxide gas mixture Download PDFInfo
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- CN211635902U CN211635902U CN201922341408.6U CN201922341408U CN211635902U CN 211635902 U CN211635902 U CN 211635902U CN 201922341408 U CN201922341408 U CN 201922341408U CN 211635902 U CN211635902 U CN 211635902U
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Abstract
The utility model relates to a mist's separation technical field discloses a piece-rate system of hydrogen chloride and sulfur dioxide mist, and piece-rate system includes absorption tower, dephlegmator and extraction pump. The utility model discloses a return line flows partial cauldron liquid back to the top of the tower, mixes the back with the process water and as the absorbent, absorbs as the absorbent with the dilute acid in other words, can restrain the sulfur dioxide and transfer to the liquid phase in. The utility model discloses a directly lead to steam at the tower cauldron, dilute and heat the gaseous phase that contains more sulfur dioxide in the hypomere tower, and steam strips the liquid phase simultaneously, makes sulfur dioxide content obviously reduce in the cauldron liquid. The utility model discloses a normal pressure equipment, and only need use a tower, equipment cost and energy consumption are all low. The utility model provides an equipment operation elasticity is big, and process design and operation maintenance are all very easy.
Description
Technical Field
The utility model relates to a separation technical field of mist especially relates to a piece-rate system of hydrogen chloride and sulfur dioxide mist.
Background
In organic synthesis, sulfuryl chloride and thionyl chloride are taken as chlorinating agents to carry out chlorination reaction, a large amount of mixed tail gas of sulfur dioxide and hydrogen chloride can be generated, the sulfur dioxide and the hydrogen chloride are valuable industrial raw materials, and direct discharge can not only pollute the environment, but also cause waste.
The commonly used tail gas treatment scheme is that multistage water absorption and alkali absorption are carried out, and finally, the acidic tail gas is converted into by-product hydrochloric acid and by-product sodium sulfite, but the process cannot satisfactorily separate hydrogen chloride from sulfur dioxide, and considerable sulfur dioxide is dissolved in the obtained by-product hydrochloric acid, so that not only is impurities introduced into the by-product hydrochloric acid during use, but also the sulfur dioxide with reducibility can directly damage some reaction systems, and a large amount of by-product hydrochloric acid and sodium sulfite cannot be properly utilized due to the purity problem, and finally, only can be neutralized and then used as wastewater for treatment.
The mixed tail gas is treated by adopting a pressure swing rectification process to obtain high-purity hydrogen chloride and sulfur dioxide, but equipment used by the pressure swing rectification process is very complicated and comprises a plurality of rectification towers and a large number of pipelines, the mixture of the liquid sulfur dioxide and the hydrogen chloride is extremely strong protonic acid, expensive corrosion-resistant materials are required to be selected for the equipment, and the equipment cost is high; and the pressure swing distillation process inevitably needs vacuum pumping operation, so the power consumption is very large.
The solubility of the sulfur dioxide in the acid is obviously reduced, the diffusion rate of the sulfur dioxide to the solution is obviously lower than that of hydrogen chloride, and the content of the sulfur dioxide in the byproduct hydrochloric acid obtained by the absorption method can be reduced by using dilute hydrochloric acid as an absorbent.
In addition, a large amount of heat is released in the hydrogen chloride dissolving process, even the solution can be boiled, the azeotropic point of the hydrogen chloride and water is 110 ℃ under normal pressure, and the molar concentration of the hydrogen chloride is 20.24%.
SUMMERY OF THE UTILITY MODEL
The utility model provides a separation system of hydrogen chloride and sulfur dioxide gas mixture.
The technical problem to be solved is that: the absorption method for treating the mixed tail gas of the sulfur dioxide and the hydrogen chloride can generate a large amount of low-purity byproduct hydrochloric acid which is difficult to utilize, and the pressure swing distillation method for treating the mixed tail gas of the sulfur dioxide and the hydrogen chloride has higher equipment cost and energy consumption.
In order to solve the technical problem, the utility model adopts the following technical scheme: the utility model provides a separation system of hydrogen chloride and sulfur dioxide gas mixture which characterized in that: comprises an absorption tower, a partial condenser and a extraction pump;
a side line feed inlet of the absorption tower is communicated with a mixed gas feed pipe;
the tower top extraction outlet of the absorption tower is communicated with the feed inlet of the partial condenser through a tower top extraction pipe, and the condensate outlet of the partial condenser is communicated with the tower top feed inlet of the absorption tower through a condensate pipe; the non-condensed steam outlet of the partial condenser is communicated with a sulfur dioxide discharge pipe;
a kettle liquid extraction outlet of the absorption tower is communicated with a liquid inlet of an extraction pump through a kettle liquid extraction pipe, and a liquid outlet of the extraction pump is communicated with a tower top feed inlet of the absorption tower through a pump rear pipe;
the absorption tower kettle is communicated with a steam feeding pipe, and the steam feeding hole is arranged higher than the liquid level of the tower kettle;
a backflow control valve is arranged on the pump rear pipe, a hydrochloric acid discharge port is arranged in front of the backflow control valve, and the hydrochloric acid discharge port is communicated with a hydrochloric acid discharge pipe; and a process water feeding hole is formed behind the backflow control valve and communicated with the process water feeding pipe.
Furthermore, the absorption tower is a packed tower, the packing layer of the packed tower is divided into two sections, the two sections comprise an upper section packing layer and a lower section packing layer, and the mixed gas feeding pipe is communicated with a lateral line feeding port, which is positioned between the upper section packing layer and the lower section packing layer, on the packed tower shell.
Further, the packed tower is a reducing tower, and the diameter of the lower section of the tower is smaller than that of the upper section of the tower; the upper section packing layer is totally arranged in the upper section tower body, the lower section packing layer is totally arranged in the lower section tower body, and the filling height of the lower section packing layer is smaller than that of the upper section packing layer.
Further, be provided with the steam feed valve on the steam inlet pipe, be provided with the gas mixture feed valve on the gas mixture inlet pipe, be provided with the top of the tower extraction valve on the top of the tower extraction pipe, be provided with the tower cauldron extraction valve on the tower cauldron extraction pipe, be provided with the process water feed valve on the process water inlet pipe, be provided with the hydrochloric acid bleeder valve on the hydrochloric acid discharging pipe.
Further, the process water feeding pipe is communicated with an acid supplementing pipe, and an acid supplementing valve is arranged on the acid supplementing pipe.
The utility model relates to a piece-rate system of hydrogen chloride and sulfur dioxide gas mixture compares with prior art, has following beneficial effect:
the utility model discloses a return line flows partial cauldron liquid back to the top of the tower, mixes the back with the process water and as the absorbent, absorbs as the absorbent with the dilute acid in other words, compares in directly absorbing with the process water, can restrain the sulfur dioxide and transfer to the liquid phase in.
The utility model discloses set up steam inlet in tower cauldron department, directly lead to steam in to the tower, dilute and heat the gaseous phase that contains more sulfur dioxide in the hypomere tower, reduce the sulfur dioxide partial pressure, promote sulfur dioxide's henry coefficient to reduce sulfur dioxide solubility, restrain its transfer in to the liquid phase, and steam strips the liquid phase simultaneously, and the sulfur dioxide that the desorption part has dissolved, sulfur dioxide content obviously reduces in the final messenger cauldron liquid.
The utility model discloses the equipment that uses is ordinary pressure equipment, and only needs to use a tower, and equipment cost and energy consumption are all low.
The utility model discloses the equipment operation elasticity of using is big, and process design and operation maintenance are all very easy.
Drawings
FIG. 1 is a schematic structural diagram of a separation system for a mixed gas of hydrogen chloride and sulfur dioxide in the present invention;
the system comprises an absorption tower 1, a liquid distributor 11, an upper section packing layer 121, a lower section packing layer 122, a dephlegmator 2, a steam feed valve 31, a mixed gas feed valve 32, a tower top extraction valve 33, a process water feed valve 341, an acid supplementing valve 342, a reflux control valve 35, a hydrochloric acid discharge valve 36, a tower bottom extraction valve 37, a 4-extraction pump 51, a steam feed pipe 51, a mixed gas feed pipe 52, a tower top extraction pipe 53, a sulfur dioxide discharge pipe 54, a condensate pipe 55, a process water feed pipe 561, a 562-acid supplementing pipe 57, a hydrochloric acid discharge pipe 581-tower liquid extraction pipe and a 582-pump rear pipe.
Detailed Description
As shown in fig. 1, the separation system of a mixed gas of hydrogen chloride and sulfur dioxide of the present invention comprises an absorption tower 1, a dephlegmator 2, and a withdrawal pump 4;
the side feed inlet of the absorption tower 1 is communicated with a mixed gas feed pipe 52; the tower kettle of the absorption tower 1 is communicated with a steam feeding pipe 51;
the tower top extraction outlet of the absorption tower 1 is communicated with the feed inlet of the partial condenser 2 through a tower top extraction pipe 53, and the condensate outlet of the partial condenser 2 is communicated with the tower top feed inlet of the absorption tower 1 through a condensate pipe 55; the non-condensed steam outlet of the partial condenser 2 is communicated with a sulfur dioxide discharge pipe 54;
the tower kettle of the absorption tower 1 is communicated with a steam feeding pipe 51, and the steam feeding hole is arranged higher than the highest liquid level line of the tower kettle; because the purpose of the steam introduction of the tower kettle in the system is steam stripping and sulfur dioxide dissolution inhibition, direct heat exchange is not realized.
A kettle liquid extraction outlet of the absorption tower 1 is communicated with a liquid inlet of an extraction pump 4 through a kettle liquid extraction pipe 581, and a liquid outlet of the extraction pump 4 is communicated with a tower top feed inlet of the absorption tower 1 through a pump rear pipe 582;
a reflux control valve 35 is arranged on the pump rear pipe 582, a hydrochloric acid discharge port is arranged in front of the reflux control valve 35, and the hydrochloric acid discharge port is communicated with a hydrochloric acid discharge pipe 57; a process water feed inlet is arranged behind the reflux control valve 35 and is communicated with a process water feed pipe 561.
The steam feed pipe 51 is provided with a steam feed valve 31, the mixed gas feed pipe 52 is provided with a mixed gas feed valve 32, the tower top extraction pipe 53 is provided with a tower top extraction valve 33, the tower bottom extraction pipe is provided with a tower bottom extraction valve 37, the process water feed pipe 561 is provided with a process water feed valve 341, and the hydrochloric acid discharge pipe 57 is provided with a hydrochloric acid discharge valve 36.
The side surface of the process water feeding pipe 561 is communicated with an acid supplementing pipe 562, an acid supplementing valve 342 is arranged on the acid supplementing pipe 562, and the acid supplementing pipe 562 is arranged for facilitating the driving.
The absorption tower 1 can be a plate tower or a packed tower, but the packed tower has a more compact structure. When the packed tower is used, the packing layer of the packed tower is divided into two sections, including an upper section packing layer 121 and a lower section packing layer 122, and the mixed gas feeding pipe 52 is communicated with a side feed inlet positioned between the upper section packing layer 121 and the lower section packing layer 122 on the shell of the packed tower. The packed tower is a reducing tower, the diameter of the lower section of the tower is smaller than that of the upper section of the tower, and the filling height of the lower section of the packing layer 122 is smaller than that of the upper section of the packing layer 121. Because in the lower section of the column, the gas phase loading is significantly reduced and the lower packing layer 122 functions primarily as stripping rather than absorption. The liquid phase feeding viscosity at the tower top is not high, and the liquid distributor 11 of the packed tower can be a spray type liquid distributor 11. In addition, since the diameter of the lower packing layer 122 is not large, the liquid redistributor may not be provided.
The cooling medium of the partial condenser 2 is desalted water, the partial condenser 2 mainly has the function of separating acid mist and partial water in the gas phase extracted from the top of the tower, the condensate is directly pumped back to the absorption tower 1, and a buffer tank can be arranged on the condensate pipe 55.
The system has great operation flexibility and allows each valve to be manually adjusted to operate without a PID control system. However, the valves may be controlled by incorporating a PID control system depending on the process design.
In the embodiment, the separation system of the mixed gas of hydrogen chloride and sulfur dioxide comprises the following steps in the driving process:
step 2, when the condensate flows in the condensate pipe 55, the process water feeding valve 341 and the acid supplementing valve 342 are opened, hydrochloric acid is introduced into the process water from the acid supplementing pipe 562, the mass flow and the acidity of the introduced hydrochloric acid are the same as those of the recycled hydrochloric acid refluxed in the normal production process, and the introduced hydrochloric acid can be the recycled hydrochloric acid produced in the system before or purchased hydrochloric acid;
step 3, opening a tower kettle extraction valve 37 when the liquid level of the kettle liquid reaches 50%; when the kettle liquid extraction pipe 581 is filled with liquid, the extraction pump 4 is started and the hydrochloric acid discharge valve 36 is opened;
and 5, opening the reflux control valve 35 and closing the acid supplementing valve 342 when the acidity of the kettle liquid meets the process design requirement.
The separation system is used for separating the mixed gas of hydrogen chloride and sulfur dioxide, water introduced from the top of the tower is used as an absorbent to carry out countercurrent absorption on the mixed gas in the absorption tower 1, sulfur dioxide gas is extracted from the top of the tower, and hydrochloric acid is extracted and recovered from the bottom of the tower; the key points of the separation process are as follows:
feeding mixed gas between an upper layer of packing and a lower layer of packing of the absorption tower 1, and directly introducing steam into a tower kettle; absorbing the gas phase in an upper section packing layer 121 of the tower to absorb the hydrogen chloride in the mixed gas; the lower packing layer 122 is stripped of the liquid phase to remove sulfur dioxide that enters the liquid phase. Note that the temperature of the recovered hydrochloric acid entering the lower packing layer 122 should be not lower than 100 ℃, i.e. the boiling point of the water under the pressure in the column; and the steam feeding temperature is not lower than 110 ℃, namely the azeotropic point of water and hydrogen chloride under the pressure in the tower; otherwise most of the stripping steam will liquefy and stripping cannot be performed. The temperature of the recovered hydrochloric acid entering the lower packing layer 122 can be controlled by controlling the process water feeding temperature, the mixed gas feeding temperature and/or the process water flow.
Condensing and dehumidifying the gas phase extracted from the tower top in a partial condenser 2, returning the condensate to the tower top, and extracting the condensate without condensing the steam completely;
part of recovered hydrochloric acid extracted from the tower bottom flows back to the tower top, and flows down from the tower top after being mixed with process water to form dilute hydrochloric acid, so that the sulfur dioxide at the tower top can be inhibited from being dissolved into a liquid phase. The reflux recovered hydrochloric acid is not directly injected into the tower, and the reflux recovered hydrochloric acid is firstly mixed with process water, the mass fraction of hydrogen chloride after the reflux recovered hydrochloric acid is mixed with the process water is less than 20%, otherwise, part of hydrogen chloride in a liquid phase at the top of the tower is volatilized into a gas phase, and a gas phase product is polluted.
And comprises the following processes: and (3) mixed gas absorption: the mixed gas is fed from a side line feed port of the absorption tower 1 and flows upwards, and is in countercurrent contact with dilute acid flowing down from the top of the tower, the mixed gas removes hydrogen chloride to become sulfur dioxide gas containing certain moisture, and the sulfur dioxide gas is extracted from the top of the tower and enters a partial condenser 2; the dilute acid absorbs hydrogen chloride and a small amount of sulfur dioxide in the mixed gas to form recovered hydrochloric acid, and the recovered hydrochloric acid is heated and continuously flows downwards;
condensing and dehumidifying sulfur dioxide: condensing sulfur dioxide gas containing certain moisture extracted from the tower top in the partial condenser 2, leading hydrochloric acid mist and most of moisture to enter condensate and return to the tower top of the absorption tower 1, and taking the sulfur dioxide gas as a gas-phase product to be extracted from a non-condensed steam outlet of the partial condenser 2;
recovering hydrochloric acid and stripping: in the tower section of the absorption tower 1 below the mixed gas feed inlet, the recovered hydrochloric acid is in countercurrent contact with steam introduced from the tower kettle, and part of sulfur dioxide in the recovered hydrochloric acid enters the steam; the steam flows upwards and converges into the mixed gas, and the recovered hydrochloric acid flows into the tower kettle and is extracted from a kettle liquid extraction outlet;
refluxing the kettle liquid: part of recovered hydrochloric acid extracted from the tower kettle is mixed with process water to form dilute hydrochloric acid, and then the dilute hydrochloric acid flows back to the top of the absorption tower 1; the rest of the recovered hydrochloric acid is taken out as a liquid phase product.
Case 1:
process water: the temperature is 40 ℃, and the flow is 13000 kg/h;
steam: 7bar of saturated steam with a flow rate of 270 Kg/h;
a partial condenser 2: the cooling medium is desalted water at 20 ℃, and the temperature of the produced non-condensed steam is 40 ℃;
mixed gas: HCl and SO2The mass ratio is 1:1, the temperature is 40 ℃, and the flow rate is 10800 kg/h;
filling: the ceramic packing, the upper section packing layer 121 is 6 meters high and 1.8 meters in diameter, and the lower section packing layer 122 is 2 meters high and 1 meter in diameter;
the liquid level of the tower bottom is controlled at 50 percent, and the reflux amount is 1300 kg/h;
in the embodiment, the mass concentration of the hydrogen chloride in the recovered hydrochloric acid extracted from the tower kettle is 30.4 percent, and the SO content is 30.4 percent2The mass concentration is 0.0451%; SO in the non-condensed steam extracted by the partial condenser 22The mass concentration is 98.2 percent, and the mass concentration reaches 99.99 percent after drying.
Case 2:
process water: the temperature is 40 ℃, and the flow is 13000 kg/h;
steam: 7bar of saturated steam with the flow rate of 440 Kg/h;
a partial condenser 2: the cooling medium is desalted water at 20 ℃, and the temperature of the produced non-condensed steam is 40 ℃;
mixed gas: HCl and SO2The mass ratio is 1:1, the temperature is 40 ℃, and the flow rate is 10800 kg/h;
filling: the ceramic packing, the upper section packing layer 121 is 6 meters high and 1.8 meters in diameter, and the lower section packing layer 122 is 2 meters high and 1 meter in diameter;
the liquid level of the tower bottom is controlled at 50 percent, and the reflux amount is 1300 kg/h;
in the embodiment, the mass concentration of hydrogen chloride in the recovered hydrochloric acid extracted from the tower kettle is 30.1 percent, and the mass concentration of SO2The mass concentration is 0.0232%; SO in the non-condensed steam extracted by the partial condenser 22The mass concentration is 98.2 percent, and the mass concentration reaches 99.99 percent after drying.
Case 3:
process water: the temperature is 40 ℃, and the flow is 13000 kg/h;
steam: 7bar of saturated steam with the flow rate of 1400 Kg/h;
a partial condenser 2: the cooling medium is desalted water at 20 ℃, and the temperature of the produced non-condensed steam is 40 ℃;
mixed gas: HCl and SO2The mass ratio is 1:1, the temperature is 40 ℃, and the flow rate is 10800 kg/h;
filling: the ceramic packing, the upper section packing layer 121 is 6 meters high and 1.8 meters in diameter, and the lower section packing layer 122 is 2 meters high and 1 meter in diameter;
the liquid level of the tower bottom is controlled at 50 percent, and the reflux amount is 1300 kg/h;
in the embodiment, the mass concentration of the hydrogen chloride in the recovered hydrochloric acid extracted from the tower kettle is 28.5 percent, and the mass concentration of the SO is 28.5 percent2The mass concentration is 0.00274 percent; SO in the non-condensed steam extracted by the partial condenser 22The mass concentration is 98.2 percent, and the mass concentration reaches 99.99 percent after drying.
Case 4:
process water: the temperature is 40 ℃, and the flow rate is 13270 kg/h;
steam: none;
a partial condenser 2: the cooling medium is desalted water at 20 ℃, and the temperature of the produced non-condensed steam is 40 ℃;
mixed gas: HCl and SO2The mass ratio is 1:1, the temperature is 40 ℃, and the flow rate is 10800 kg/h;
filling: the ceramic packing, the upper section packing layer 121 is 6 meters high and 1.8 meters in diameter, and the lower section packing layer 122 is 2 meters high and 1 meter in diameter;
the liquid level of the tower bottom is controlled at 50 percent, and the reflux amount is 1300 kg/h;
in the embodiment, the mass concentration of the hydrogen chloride in the recovered hydrochloric acid extracted from the tower kettle is 30.4 percent, and the SO content is 30.4 percent2The mass concentration is 1.01 percent; SO in the non-condensed steam extracted by the partial condenser 22The mass concentration is 98.2 percent, and the mass concentration reaches 99.99 percent after drying.
Case 5:
process water: the temperature is 20 ℃, and the flow is 13000 kg/h;
steam: 7bar of saturated steam with a flow rate of 270 Kg/h;
a partial condenser 2: the cooling medium is desalted water at 20 ℃, and the temperature of the produced non-condensed steam is 40 ℃;
mixed gas: HCl and SO2The mass ratio is 1:1, the temperature is 40 ℃, and the flow rate is 10800 kg/h;
filling: the ceramic packing, the upper section packing layer 121 is 6 meters high and 1.8 meters in diameter, and the lower section packing layer 122 is 2 meters high and 1 meter in diameter;
the liquid level of the tower bottom is controlled at 50 percent, and the reflux amount is 1300 kg/h;
in the embodiment, the mass concentration of the hydrogen chloride in the recovered hydrochloric acid extracted from the tower kettle is 30.4 percent, and the SO content is 30.4 percent2The mass concentration is 1.01 percent; SO in the non-condensed steam extracted by the partial condenser 22The mass concentration is 98.2 percent, and the mass concentration reaches 99.99 percent after drying.
Case 6:
process water: the temperature is 40 ℃, and the flow is 13000 kg/h;
steam: 7bar of saturated steam with a flow rate of 270 Kg/h;
a partial condenser 2: the cooling medium is desalted water at 20 ℃, and the temperature of the produced non-condensed steam is 40 ℃;
mixed gas: SO (SO)2The flow rate is 5400kg/h, and the HCl flow rate is 3000 kg/h;
filling: the ceramic packing, the upper section packing layer 121 is 6 meters high and 1.8 meters in diameter, and the lower section packing layer 122 is 2 meters high and 1 meter in diameter;
the liquid level of the tower bottom is controlled at 50 percent, and the reflux amount is 1300 kg/h;
in the embodiment, the mass concentration of the hydrogen chloride in the recovered hydrochloric acid extracted from the tower kettle is 20.5 percent, and the mass concentration of the SO2The mass concentration is 1.62%; SO in the non-condensed steam extracted by the partial condenser 22The mass concentration is 98.2 percent, and the mass concentration reaches 99.99 percent after drying.
The above-mentioned embodiments are only described for the preferred embodiments of the present invention, but not for limiting the scope of the present invention, and without departing from the design spirit of the present invention, the ordinary skilled person in the art can make various modifications and improvements to the technical solution of the present invention, including the application of the present invention in other mixed gases, all fall into the protection scope defined by the claims of the present invention.
Claims (5)
1. The utility model provides a separation system of hydrogen chloride and sulfur dioxide gas mixture which characterized in that: comprises an absorption tower (1), a partial condenser (2) and a extraction pump (4);
a side line feed inlet of the absorption tower (1) is communicated with a mixed gas feed pipe (52);
the tower top extraction outlet of the absorption tower (1) is communicated with the feeding hole of the partial condenser (2) through a tower top extraction pipe (53), and the condensate outlet of the partial condenser (2) is communicated with the tower top feeding hole of the absorption tower (1) through a condensate pipe (55); the non-condensed steam outlet of the partial condenser (2) is communicated with a sulfur dioxide discharge pipe (54);
a kettle liquid extraction outlet of the absorption tower (1) is communicated with a liquid inlet of an extraction pump (4) through a kettle liquid extraction pipe (581), and a liquid outlet of the extraction pump (4) is communicated with a tower top feed inlet of the absorption tower (1) through a pump rear pipe (582);
the tower kettle of the absorption tower (1) is communicated with a steam feeding pipe (51), and a steam feeding hole is arranged higher than the liquid level of the tower kettle;
a backflow control valve (35) is arranged on the pump rear pipe (582), a hydrochloric acid discharge hole is formed in the front of the backflow control valve (35), and the hydrochloric acid discharge hole is communicated with a hydrochloric acid discharge pipe (57); and a process water feeding hole is formed in the back of the backflow control valve (35) and communicated with a process water feeding pipe (561).
2. The system for separating the mixed gas of the hydrogen chloride and the sulfur dioxide as claimed in claim 1, characterized in that: the absorption tower (1) is a packed tower, a packing layer of the packed tower is divided into two sections and comprises an upper section packing layer (121) and a lower section packing layer (122), and the mixed gas feeding pipe (52) is communicated with a lateral line feeding port, which is positioned between the upper section packing layer (121) and the lower section packing layer (122), on a shell of the packed tower.
3. The system for separating the mixed gas of the hydrogen chloride and the sulfur dioxide as claimed in claim 2, characterized in that: the packed tower is a reducing tower, and the tower diameter of the lower section is smaller than that of the upper section; the upper section packing layer (121) is completely arranged in the upper section tower body, the lower section packing layer (122) is completely arranged in the lower section tower body, and the filling height of the lower section packing layer (122) is smaller than that of the upper section packing layer (121).
4. A separation system of a mixed gas of hydrogen chloride and sulfur dioxide according to any one of claims 1 to 3, characterized in that: the device is characterized in that a steam feed valve (31) is arranged on the steam feed pipe (51), a mixed gas feed valve (32) is arranged on the mixed gas feed pipe (52), a tower top extraction valve (33) is arranged on the tower top extraction pipe (53), a tower kettle extraction valve (37) is arranged on the tower kettle extraction pipe, a process water feed valve (341) is arranged on the process water feed pipe (561), and a hydrochloric acid discharge valve (36) is arranged on the hydrochloric acid discharge pipe (57).
5. The system for separating the mixed gas of hydrogen chloride and sulfur dioxide as claimed in claim 4, wherein: the process water feeding pipe (561) is communicated with an acid supplementing pipe (562), and an acid supplementing valve (342) is arranged on the acid supplementing pipe (562).
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