CN211216061U - Contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery unit - Google Patents
Contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery unit Download PDFInfo
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- CN211216061U CN211216061U CN201921092628.3U CN201921092628U CN211216061U CN 211216061 U CN211216061 U CN 211216061U CN 201921092628 U CN201921092628 U CN 201921092628U CN 211216061 U CN211216061 U CN 211216061U
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Abstract
The utility model discloses a contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery unit and technology, it contains hydrogen fluoride and hydrogen chloride tail gas condensation recovery unit, including the liquid nitrogen condenser ware, it is used for carrying out the condensation with waste gas, the air inlet and the import intercommunication of waste gas intercommunication, gas outlet and adsorption equipment or compressor of liquid nitrogen condenser, the liquid outlet of liquid nitrogen condenser and the import intercommunication of depositing the jar to with the liquid HF input storage in the storage jar after the liquid nitrogen condenser condensation. The utility model discloses the flow is simple, and is high to HF, HCL's separation efficiency, and can create economic value, reduces the high-priced cost problem that exhaust-gas treatment brought.
Description
Technical Field
The utility model relates to a waste gas treatment technique in the lithium hexafluorophosphate production process especially relates to a contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery unit.
Background
Lithium hexafluorophosphate is an important raw material (electrolyte) of a new energy battery, a large amount of anhydrous hydrogen fluoride and hydrogen chloride gas are generated in the production process of lithium hexafluorophosphate, the existing treatment method is to absorb the anhydrous hydrogen fluoride and the hydrogen chloride gas into fluorine-containing hydrochloric acid or treat the fluorine-containing hydrochloric acid as wastewater, resources are seriously wasted, and the economic benefit of an enterprise is influenced.
SUMMERY OF THE UTILITY MODEL
In view of the above-mentioned defect of prior art, the utility model aims to solve the technical problem that a contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery device and technology are provided, it can carry out recycle to the waste gas in the lithium hexafluorophosphate production process.
In order to realize the above purpose, the utility model provides a contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery unit, including the liquid nitrogen condenser ware, it is used for carrying out the condensation with waste gas, the air inlet of liquid nitrogen condenser ware and the import intercommunication of waste gas intercommunication, gas outlet and adsorption equipment or compressor, the liquid outlet of liquid nitrogen condenser ware and the import intercommunication of storage tank to with the storage in the liquid HF input storage tank after the liquid nitrogen condenser condensation.
Preferably, the compressor is used for compressing gaseous HCL, and then storing the gaseous HCL through a gas cylinder to obtain industrial-grade steel cylinder gas.
Preferably, the adsorption device is used for adsorbing HF in gas, and high-purity HCL is compressed into a gas cylinder by a compressor to obtain high-purity grade cylinder gas.
Preferably, the adsorption device comprises two alumina adsorption tanks, one of the two alumina adsorption tanks is used, the alumina adsorption tank comprises an outer box and an inner box, the inner box is arranged in the outer box, a heat preservation gap is formed between the inner box and the inner wall of the outer box, and a first coil is arranged in the heat preservation gap;
at least two heating plates are fixed in the inner box, air passing holes and heating strips are arranged on the heating plates, and the inner box is filled with alumina for adsorbing VOC; the top of the inner side of the inner box is respectively communicated with one end of a first auxiliary access pipe, one end of a second auxiliary access pipe and one end of a third auxiliary access pipe;
the air inlet pipe is communicated with an inlet of a first reversing valve, a first outlet and a second outlet of the first reversing valve are respectively communicated with the other ends of first auxiliary access pipes of the two alumina adsorption tanks, and the first reversing valve is used for selecting one of the inlets to be communicated with one of the first auxiliary access pipes when in use; the first access pipe is communicated with an inlet of the first one-way valve, and an outlet of the first one-way valve is communicated with the exhaust pipe, so that the treated gas is output.
Preferably, the second auxiliary access pipe is communicated with an inlet of a fourth one-way valve, an outlet of the fourth one-way valve is communicated with a condensation access port of a condenser, and a condensation access outlet of the condenser is communicated with an inlet of the storage tank; the second access pipe is communicated with an inlet of a second one-way valve, and an outlet of the second one-way valve is communicated with an inlet of the storage tank; and the third auxiliary access pipe is communicated with an inlet of a third one-way valve, and an outlet of the third one-way valve is communicated with a condensation access port of the condenser.
Preferably, the other ends of the third access pipes of the two alumina adsorption tanks are respectively communicated with a first outlet and a second outlet of a second reversing valve, an inlet of the second reversing valve is communicated with an outlet of a steam pump, the steam pump belongs to a steam system, the steam system further comprises a booster water pump, an inlet of the booster water pump is communicated with a water source, an outlet of the booster water pump is communicated with an inlet of an atomizer, the atomizer is used for atomizing water, an outlet of the atomizer is communicated with a first inlet of a third reversing valve, a second inlet of the third reversing valve is communicated with an external air source, an outlet of the third reversing valve is communicated with one end of a heating gap of a heater, and the third reversing valve is used for selecting one to enable the first inlet and the second inlet to be communicated with the outlet of the third reversing valve;
the heater comprises a second shell and a second shell, an installation gap is formed between the first shell and the second shell, a second coil is installed in the installation gap, first heating baffles and second heating baffles which are arranged in a staggered mode are installed in the second shell, a heating gap is formed between the first heating baffles and the second heating baffles, and the other end of the heating gap is communicated with an inlet of the steam pump;
the first heating baffle and the second heating baffle are made of iron materials, alternating current is introduced into the second coil, and one of the second reversing valves is communicated with one of the third access pipes.
Preferably, the heat insulation gap is filled with a heat insulation material; the installation gap is filled with heat insulation cotton.
The utility model also discloses a contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery technology, including following step:
s1, inputting the waste gas of the mixed oil HF and the HCL into a liquid nitrogen condenser, and cooling the waste gas to-98 ℃ through the liquid nitrogen condenser to liquefy the HF and keep the HCL in a gaseous state;
and S2, outputting and storing the liquid phase, and outputting the separated gas for further processing.
Preferably, in S2, the separated gas is fed into a compressor, compressed and bottled to obtain industrial grade HCL steel cylinder gas.
Preferably, in S2, the separated gas is adsorbed by a multi-stage alumina adsorption tank to obtain high-purity HCL, so as to obtain high-purity HCL gas.
The utility model has the advantages that: the utility model discloses the flow is simple, and is high to HF, HCL's separation efficiency, and can create economic value, reduces the high-priced cost problem that exhaust-gas treatment brought.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic structural view of the adsorption device of the present invention.
Fig. 3 is an enlarged view at F1 in fig. 2.
Fig. 4 is a schematic diagram of the steam system of the present invention.
Detailed Description
The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
Referring to fig. 1, the tail gas condensation and recovery device containing hydrogen fluoride and hydrogen chloride of the embodiment includes a liquid nitrogen condenser for condensing the waste gas, wherein an air inlet of the liquid nitrogen condenser is communicated with the waste gas, an air outlet of the liquid nitrogen condenser is communicated with an inlet of an adsorption device or a compressor, and a liquid outlet of the liquid nitrogen condenser is communicated with an inlet of a storage tank, so that the liquid HF condensed by the liquid nitrogen condenser is input into the storage tank for storage;
the compressor is used for compressing gaseous HCL and then storing the gaseous HCL through a gas cylinder to obtain industrial-grade steel cylinder gas. The adsorption device is used for adsorbing HF in gas so as to purify HCL, and high-purity gas is compressed into a gas cylinder through a compressor to obtain high-purity steel cylinder gas.
The specific process is as follows:
because the boiling point of HF is 19.5 ℃ and the boiling point of HCL is 85 ℃, the utility model utilizes the difference between the boiling points of the HF and the HCL, and the temperature of the mixed gas (tail gas) is reduced to-98 ℃ by a liquid nitrogen condenser so as to separate the HF and the HCL; 85.12 percent of hydrogen fluoride is obtained from the liquid phase, the recovery rate of the hydrogen fluoride is 99.9 percent, and the method can be used for producing lithium hexafluorophosphate. The gas phase of 99.8% HCl (containing less than 20ppm of HF) is compressed and bottled for sale as industrial grade HCl steel cylinder gas.
If after the liquid nitrogen is condensed, the adsorption tank containing multi-stage alumina is used for adsorption to remove HF, the purity of HCL can reach 99.999%, and the trace impurity value is controlled below 5ppm, so that the standard of high-purity HCL gas can be reached.
Referring to fig. 2 to 4, although the amount of HF adsorbed by alumina in the alumina adsorption tank is small, the alumina adsorption tank needs to be replaced during continuous production to ensure the adsorption effect. Aluminum fluoride can be generated after the aluminum oxide absorbs HF, aluminum fluoride can be partially hydrolyzed at 30-400 ℃ to generate aluminum oxide and HF, if a recycling mode of hydrolyzing the aluminum oxide is adopted, the replacement frequency of an aluminum oxide adsorption tank can be greatly reduced, solid wastes such as the generated aluminum fluoride and the generated aluminum oxide are also reduced, and most of the hydrolyzed HF can be recycled. And other impurities are contained in the condensed gas, and the impurities can be filtered by an alumina adsorption tank.
However, uninterrupted production is guaranteed, therefore, the applicant sets two alumina adsorption tanks for each adsorption device, the adsorption device comprises two alumina adsorption tanks, the two alumina adsorption tanks are alternatively used, the alumina adsorption tanks comprise an outer tank a110 and an inner tank a120, the inner tank a120 is installed inside the outer tank a110, a heat preservation gap a111 is formed between the inner tank a120 and the inner wall of the outer tank a110, a first coil a210 is installed in the heat preservation gap a111, a heat preservation material a411 is filled in the heat preservation gap a111, and the heat preservation material a411 is a heat insulation material, such as heat insulation foam.
At least two heating plates A130 are fixed in the inner box A120, air passing holes A131 and heating strips A132 are arranged on the heating plates A130, the inner box A120 is filled with alumina A412, and the alumina A412 is used for adsorbing VOC. The heating plate and the heating strip are made of ferrous materials, alternating current is introduced into the first coil A210, so that an alternating magnetic field is generated, and the heating plate A130 generates heat through the alternating magnetic field to heat the aluminum oxide.
The top of the inner side of the inner box A120 is respectively communicated with one end of a first auxiliary access pipe A151, one end of a second auxiliary access pipe A152 and one end of a third auxiliary access pipe A153, and the bottom of the inner side of the inner box A120 is respectively communicated with one end of a first access pipe A141, one end of a second access pipe A142 and one end of a third access pipe A143;
the gas inlet pipe 110 is communicated with an inlet of a first reversing valve A211, a first outlet and a second outlet of the first reversing valve A211 are respectively communicated with the other ends of first auxiliary access pipes A151 of the two alumina adsorption tanks, and when the gas inlet pipe is used, the first reversing valve A211 is used for selecting one of the first auxiliary access pipes A151 to communicate the inlet of the first auxiliary access pipe A211 with one of the first auxiliary access pipes A151, so that heat exchange gas exhausted by the heat exchanger 150 is conveyed into one of the alumina adsorption tanks.
The first inlet pipe a141 communicates with an inlet of the first check valve a221, and an outlet of the first check valve a221 communicates with the exhaust pipe 120, thereby outputting the treated gas. The second auxiliary access pipe a152 is communicated with an inlet of a fourth one-way valve a224, an outlet of the fourth one-way valve a224 is communicated with a condensation access port of a condenser a250, and a condensation access port of the condenser a250 is communicated with an inlet of a storage tank a260, so that condensed water flows back to the storage tank a260 to be stored.
The second access pipe a142 is communicated with an inlet of a second one-way valve a222, and an outlet of the second one-way valve a222 is communicated with an inlet of the storage tank a260, so that the liquid during hydrolysis flows into the storage tank a260 for storage.
The third auxiliary access pipe A153 is communicated with an inlet of a third one-way valve A223, an outlet of the third one-way valve A223 is communicated with a condensation access port of a condenser A250, so that water vapor generated during drying is condensed, and the condensed gas is directly discharged or input into the air inlet pipe 110 for further treatment;
the other ends of third access pipes A143 of the two alumina adsorption tanks are respectively communicated with a first outlet and a second outlet of a second reversing valve A212, an inlet of the second reversing valve A212 is communicated with an outlet of a steam pump A273, the steam pump A273 belongs to a steam system, the steam system further comprises a booster water pump A271, an inlet of the booster water pump A271 is communicated with a water source, an outlet of the booster water pump A271 is communicated with an inlet of an atomizer A272, the atomizer A272 is used for atomizing water, an outlet of the atomizer A272 is communicated with a first inlet of a third reversing valve A213, a second inlet of the third reversing valve A213 is communicated with an external air source (atmosphere), an outlet of the third reversing valve A213 is communicated with one end of a heating gap A333 of a heater A300, and the third reversing valve A213 is used for selecting one to ensure that the first inlet and the second inlet are communicated with the outlet thereof;
the heater A300 comprises a first shell A310 and a second shell A320, wherein an installation gap A311 is formed between the first shell A310 and the second shell A320, a second coil A280 is installed in the installation gap A311, heat insulation cotton A420 is filled in the installation gap A311, a first heating baffle A331 and a second heating baffle A332 which are arranged in a staggered mode are installed in the second shell A320, a heating gap A333 is formed between the first heating baffle A331 and the second heating baffle A332, and the other end of the heating gap A333 is communicated with an inlet of a steam pump A273;
the first heating baffle A331 and the second heating baffle A332 are made of iron materials, alternating current is introduced into the second coil, so that an alternating magnetic field is generated, the alternating magnetic field enables the first heating baffle A331 and the second heating baffle A332 to generate heat, atomized water vapor is heated by the generated heat to be rapidly changed into water vapor, the water vapor is output to the second reversing valve A212 through the steam pump A273, and one of the third access pipes A143 is selected from the second reversing valve A212.
In this embodiment, when in use, the first reversing valve connects the air inlet pipe 110 with the first sub-inlet pipe a151 of the left alumina adsorption tank, and the air flow enters the alumina adsorption tank, is filtered, and then is discharged to the exhaust pipe 120 through the first inlet pipe a141 and the first check valve a221, and then is conveyed to the compressor for compression.
When the alumina adsorption tank needs hydrolysis, the first reversing valve A211 cuts off the communication with the first auxiliary access pipe A151 of the alumina adsorption tank, and communicates with the first auxiliary access pipe A151 of another alumina adsorption tank (the right alumina adsorption tank); then the airflow is discharged to a compressor or a next-stage adsorption device after being treated by the right-side alumina adsorption tank.
Meanwhile, the inlet of the second reversing valve is communicated with the third access pipe A143 of the left alumina adsorption tank, the booster water pump A271, the second coil A280, the first coil A210, the steam pump A273 and the condenser A250 are all electrified and started, the booster pump A271 boosts water and inputs the water into the atomizer to be atomized into water mist, then the water mist enters the heating gap A333 under the negative pressure generated by the steam pump A273 on the heating gap A333, the first heating baffle A331 and the second heating baffle A332 are respectively heated, then the water mist is heated by self-generated heat, the water mist is rapidly changed into high-temperature water vapor, then the high-temperature water vapor enters the steam pump A273, the steam pump A273 washes alumina by the high-temperature water vapor, the alumina is filled with VOC adsorbed by the hydrolyzed alumina, the liquid generated in the hydrolysis flows into the storage tank A260 through the second access pipe A142, the gas generated in the hydrolysis respectively enters the condenser, the condensed gas is discharged to the waste gas treatment device for treatment, The liquid is input into a storage tank for storage. In the process, the alternating magnetic field generated by the first coil heats the heating plate, and the heating plate rapidly heats the mixture of the aluminum oxide and the aluminum fluoride to 300-.
After the hydrolysis of the water vapor is completed, an external air source of a third reversing valve A213 is communicated with a heating gap A333, an atomizer A272 is disconnected from the heating gap, then a steam pump is started, external air is pumped into the heating gap and heated into high-temperature air, the high-temperature air dries the alumina, a booster water pump A271, a second coil A280, a first coil A210, a steam pump A273 and a condenser A250 respectively stop running after drying, the hydrolysis is completed, and the alumina adsorption tank after hydrolysis enters a standby state and repeats the steps.
This kind of design makes the utility model discloses can realize uninterrupted work to increase of production, reduce cost, the hydrolysis of aluminium fluoride can increase aluminium oxide life moreover, thereby reduces solid useless, reduction in use cost.
The details of the present invention are well known to those skilled in the art.
The foregoing has described in detail preferred embodiments of the present invention. It should be understood that numerous modifications and variations can be devised by those skilled in the art in light of the teachings of the present invention without undue experimentation. Therefore, the technical solutions that can be obtained by a person skilled in the art through logic analysis, reasoning or limited experiments based on the prior art according to the concepts of the present invention should be within the scope of protection defined by the claims.
Claims (5)
1. The utility model provides a contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery unit which characterized by: the waste gas treatment device comprises a liquid nitrogen condenser, wherein the liquid nitrogen condenser is used for condensing waste gas, an air inlet of the liquid nitrogen condenser is communicated with the waste gas, an air outlet of the liquid nitrogen condenser is communicated with an inlet of an adsorption device or a compressor, and a liquid outlet of the liquid nitrogen condenser is communicated with an inlet of a storage tank, so that liquid HF condensed by the liquid nitrogen condenser is input into the storage tank for storage.
2. The apparatus for condensing and recovering tail gas containing hydrogen fluoride and hydrogen chloride as set forth in claim 1, wherein: the adsorption device comprises two alumina adsorption tanks, one of the two alumina adsorption tanks is used, the alumina adsorption tank comprises an outer box and an inner box, the inner box is arranged in the outer box, a heat preservation gap is formed between the inner box and the inner wall of the outer box, and a first coil is arranged in the heat preservation gap;
at least two heating plates are fixed in the inner box, air passing holes and heating strips are arranged on the heating plates, and the inner box is filled with alumina for adsorbing VOC; the top of the inner side of the inner box is respectively communicated with one end of a first auxiliary access pipe, one end of a second auxiliary access pipe and one end of a third auxiliary access pipe;
the air inlet pipe is communicated with an inlet of a first reversing valve, a first outlet and a second outlet of the first reversing valve are respectively communicated with the other ends of first auxiliary access pipes of the two alumina adsorption tanks, and the first reversing valve is used for selecting one of the inlets to be communicated with one of the first auxiliary access pipes when in use; the first access pipe is communicated with an inlet of the first one-way valve, and an outlet of the first one-way valve is communicated with the exhaust pipe, so that the treated gas is output.
3. The apparatus for condensing and recovering tail gas containing hydrogen fluoride and hydrogen chloride as claimed in claim 2, wherein: the second auxiliary access pipe is communicated with an inlet of a fourth one-way valve, an outlet of the fourth one-way valve is communicated with a condensation access port of a condenser, and a condensation access port of the condenser is communicated with an inlet of the storage tank; the second access pipe is communicated with an inlet of a second one-way valve, and an outlet of the second one-way valve is communicated with an inlet of the storage tank; and the third auxiliary access pipe is communicated with an inlet of a third one-way valve, and an outlet of the third one-way valve is communicated with a condensation access port of the condenser.
4. The apparatus for condensing and recovering a tail gas containing hydrogen fluoride and hydrogen chloride as set forth in claim 3, wherein: the other ends of third access pipes of the two alumina adsorption tanks are respectively communicated with a first outlet and a second outlet of a second reversing valve, an inlet of the second reversing valve is communicated with an outlet of a steam pump, the steam pump belongs to a steam system, the steam system further comprises a booster water pump, an inlet of the booster water pump is communicated with a water source, an outlet of the booster water pump is communicated with an inlet of an atomizer, the atomizer is used for atomizing water, an outlet of the atomizer is communicated with a first inlet of a third reversing valve, a second inlet of the third reversing valve is communicated with an external air source, an outlet of the third reversing valve is communicated with one end of a heating gap of a heater, and the third reversing valve is used for selecting one to enable the first inlet and the second inlet to be communicated with the outlet of the third reversing valve;
the heater comprises a second shell and a second shell, an installation gap is formed between the first shell and the second shell, a second coil is installed in the installation gap, first heating baffles and second heating baffles which are arranged in a staggered mode are installed in the second shell, a heating gap is formed between the first heating baffles and the second heating baffles, and the other end of the heating gap is communicated with an inlet of the steam pump;
the first heating baffle and the second heating baffle are made of iron materials, alternating current is introduced into the second coil, and one of the second reversing valves is communicated with one of the third access pipes.
5. The apparatus for condensing and recovering tail gas containing hydrogen fluoride and hydrogen chloride as set forth in claim 4, wherein: the heat insulation gap is filled with heat insulation materials; the installation gap is filled with heat insulation cotton.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921092628.3U CN211216061U (en) | 2019-07-12 | 2019-07-12 | Contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery unit |
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| CN201921092628.3U CN211216061U (en) | 2019-07-12 | 2019-07-12 | Contain hydrogen fluoride and hydrogen chloride tail gas condensation recovery unit |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112206631A (en) * | 2019-07-12 | 2021-01-12 | 上海协柯环保设备有限公司 | Condensation recovery device and process for tail gas containing hydrogen fluoride and hydrogen chloride |
| CN112604431A (en) * | 2020-11-19 | 2021-04-06 | 衡阳鸿宇化工有限责任公司 | Tail gas treatment device for aluminum trichloride production and use method thereof |
| CN114477114A (en) * | 2022-01-25 | 2022-05-13 | 上海协柯环保设备有限公司 | Equipment and method for rectifying, separating and purifying mixed gas of hydrogen fluoride, phosphorus pentafluoride and hydrogen chloride |
-
2019
- 2019-07-12 CN CN201921092628.3U patent/CN211216061U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112206631A (en) * | 2019-07-12 | 2021-01-12 | 上海协柯环保设备有限公司 | Condensation recovery device and process for tail gas containing hydrogen fluoride and hydrogen chloride |
| CN112604431A (en) * | 2020-11-19 | 2021-04-06 | 衡阳鸿宇化工有限责任公司 | Tail gas treatment device for aluminum trichloride production and use method thereof |
| CN114477114A (en) * | 2022-01-25 | 2022-05-13 | 上海协柯环保设备有限公司 | Equipment and method for rectifying, separating and purifying mixed gas of hydrogen fluoride, phosphorus pentafluoride and hydrogen chloride |
| CN114477114B (en) * | 2022-01-25 | 2024-01-26 | 上海协柯环保设备有限公司 | Equipment and method for rectifying, separating and purifying mixed gas of hydrogen fluoride, phosphorus pentafluoride and hydrogen chloride |
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