CN107010599B - Sodium hypochlorite continuous production device - Google Patents
Sodium hypochlorite continuous production device Download PDFInfo
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- CN107010599B CN107010599B CN201710201106.1A CN201710201106A CN107010599B CN 107010599 B CN107010599 B CN 107010599B CN 201710201106 A CN201710201106 A CN 201710201106A CN 107010599 B CN107010599 B CN 107010599B
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- C01B11/00—Oxides or oxyacids of halogens; Salts thereof
- C01B11/04—Hypochlorous acid
- C01B11/06—Hypochlorites
- C01B11/062—Hypochlorites of alkali metals
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a sodium hypochlorite continuous production device, which comprises: the device comprises N front-stage absorption towers, N storage containers, a tail gas absorption tower and a dilute alkali storage tank, wherein the N storage containers, the tail gas absorption tower and the dilute alkali storage tank are in one-to-one correspondence with the N front-stage absorption towers, and N is larger than or equal to 1; output pipes are arranged on the storage container and the dilute alkali storage tank, and a suction pump and a cooler are arranged on the output pipes. The continuous sodium hypochlorite production device provided by the invention has the advantages that the chlorine flow direction is opposite to the weak alkali flow direction, and the chlorine and the weak alkali are in reverse contact. In this way, the chlorine with the highest purity reacts with the mixed solution with the lowest alkali solution content, then the mixed gas with the gradually reduced chlorine content contacts with the mixed liquid with the gradually increased alkali solution content, and finally the unreacted chlorine with the extremely low content in the gas is directly mixed with the light alkali in the absorption tower. Thus, the absorption of chlorine is ensured, the cost is saved, and the pollution problem of tail gas emission is solved.
Description
Technical Field
The invention relates to the technical field of chemical product production devices, in particular to a sodium hypochlorite continuous production device.
Background
Sodium hypochlorite is a high-efficiency oxidant and chlorine-containing disinfectant, and is used as bleaching agent, oxidant and water purifying agent for paper making, textile, light industry and the like, and is used as chlorinating agent for oxidizing and synthesizing hydrazine hydrate, azodicarbonamide and chloroisocyanuric acid in the production of organic chemical products. As one of the products of chlor-alkali industry, sodium hypochlorite production is a branch of chlor-alkali industry, and is generally produced by adopting a caustic soda chlorination method, namely chlorine and caustic soda are reacted under the condition of low temperature (below 15 ℃), and the production method comprises a batch method and a continuous method. Batch production is currently used in the market, namely, a reaction kettle with a cooling coil is adopted, and chlorine is directly introduced into sodium hydroxide solution for reaction to obtain sodium hypochlorite solution.
The production device is an open system, and has the defects of unstable quality of sodium hypochlorite solution, difficult control of effective chlorine concentration, incomplete absorption of chlorine and the like caused by poor working reliability and low heat exchange efficiency of the cooling coil and incapability of timely removing reaction heat. In addition, when producing, chlorine and sodium hydroxide solution rely on compressed air bubbling to mix, and the reaction terminal relies on artifical sample analysis, and the effect is relatively poor, and reation kettle gaseous phase can not effectively retrieve, and environmental pollution is serious, causes the injury to operating personnel health.
Therefore, from the actual condition of the production process, the device capable of realizing continuous production and tail gas recovery is developed, so that the device has great safety, environmental protection and economic benefits, and provides references for production of other products in the chemical industry.
Disclosure of Invention
Based on the technical problems in the background technology, the invention provides a sodium hypochlorite continuous production device.
The invention provides a sodium hypochlorite continuous production device, which comprises: the device comprises N front-stage absorption towers, N storage containers, a tail gas absorption tower and a dilute alkali storage tank, wherein the N storage containers, the tail gas absorption tower and the dilute alkali storage tank are in one-to-one correspondence with the N front-stage absorption towers, and N is larger than or equal to 1;
output pipes are arranged on the storage container and the dilute alkali storage tank, and a suction pump and a cooler are arranged on the output pipes;
the tail gas absorption tower is provided with a tail gas inlet, a tail gas discharge port, a light alkali inlet and a primary product discharge port, and the primary product discharge port, the tail gas inlet, the light alkali inlet and the tail gas discharge port are sequentially arranged from bottom to top; each front section absorption tower is provided with a chlorine inlet, a chlorine outlet, a liquid inlet and a liquid outlet, wherein the liquid outlet, the chlorine inlet, the liquid inlet and the chlorine outlet are sequentially arranged from bottom to top;
the N front-stage absorption towers are sequentially arranged, a chlorine inlet of the first front-stage absorption tower is connected with a chlorine supply device, chlorine inlets of the rest front-stage absorption towers are all connected with a chlorine outlet of the front-stage absorption tower, and a chlorine outlet of the last front-stage absorption tower is connected with a tail gas inlet of the tail gas absorption tower; the alkali liquor inlet of the tail gas absorption tower is communicated with the output pipe of the dilute alkali storage tank; the primary product discharge port of the tail gas absorption tower is communicated with the last storage container, the liquid outlet of each front section absorption tower is communicated with the corresponding storage container, the output pipe of the Mth storage container is communicated with the liquid inlet of the Mth-1 front section absorption tower, M is more than or equal to 2 and less than or equal to N, the output pipe of the Nth storage container is also communicated with the liquid inlet of the Nth front section absorption tower, and the output pipe of the first front section absorption tower is connected to a secondary acid finished product tank;
the top of the storage container is provided with a tail gas outlet which is communicated with a tail gas inlet of the tail gas absorption tower.
Preferably, a discharge valve is arranged at the liquid outlet of the last front section absorption tower.
Preferably, each front section absorption tower is internally provided with a packing layer, and the chlorine inlet and the liquid inlet are respectively positioned below and above the packing layer.
Preferably, a packing layer is arranged in the tail gas absorption tower, the tail gas inlet and the dilute alkali inlet are respectively positioned below and above the packing layer.
Preferably, at least one tray is arranged above the packing layer in the tail gas absorption tower, a light alkali inlet is arranged on the tail gas absorption tower corresponding to each tray, and a light alkali inlet is also arranged between the packing layer and the tray on the tail gas absorption tower.
Preferably, the secondary acid finished product tank is also provided with an exhaust outlet communicated with the exhaust inlet of the exhaust gas absorption tower.
Preferably, an exhaust pump is installed at the exhaust gas discharge port.
Preferably, the cooler is a plate cooler, and the cooler input port is connected with the cooling water input device, and the cooler output port is connected with the cooling water discharge device.
Preferably, the mixer is also provided with an input port for inputting clean water and alkali liquor, and an output port of the mixer is communicated with the weak alkali storage tank.
Preferably, the device comprises two front-stage absorption towers, which are respectively called a first-stage absorption tower and a second-stage absorption tower, and storage containers corresponding to the first-stage absorption tower and the second-stage absorption tower are respectively called a finished product storage tank and a semi-finished product storage tank; the chlorine inlet of the first-stage absorption tower is connected with a chlorine supply device, the chlorine outlet of the first-stage absorption tower is communicated with the chlorine inlet of the second-stage absorption tower, and the chlorine outlet of the second-stage absorption tower is communicated with the tail gas inlet; the output pipe of the dilute alkali storage tank is communicated with the dilute alkali inlet of the tail gas absorption tower, and the primary product discharge port of the tail gas absorption tower and the liquid outlet of the two-stage absorption tower are both communicated with the semi-finished product storage tank; the output pipe of the semi-finished product storage tank is respectively communicated with the liquid inlet of the first-stage absorption tower and the liquid inlet of the second-stage absorption tower; the liquid outlet of the second section of absorption tower is communicated with a semi-finished product storage tank, and the liquid outlet of the first section of absorption tower is communicated with a finished product storage tank; the output pipe of the finished product storage tank is communicated with the secondary acid finished product tank;
the top of the semi-finished product storage tank and the top of the finished product storage tank are respectively provided with an exhaust outlet and are respectively communicated with the tail gas inlet of the tail gas absorption tower.
The continuous sodium hypochlorite production device provided by the invention has the advantages that the chlorine flow direction is opposite to the weak alkali flow direction, and the chlorine and the weak alkali are in reverse contact. In this way, the chlorine with the highest purity reacts with the mixed solution with the lowest alkali solution content, then the mixed gas with the gradually reduced chlorine content contacts with the mixed liquid with the gradually increased alkali solution content, and finally the unreacted chlorine with the extremely low content in the gas is directly mixed with the light alkali in the absorption tower. Thus, the absorption of chlorine is ensured, the cost is saved, and the pollution problem of tail gas emission is solved.
In the invention, the cooler on the output pipe of the dilute alkali storage tank is used for cooling the dilute alkali mixed by 32% alkali liquor and water, so that the low-temperature reaction of the dilute alkali and chlorine is ensured; and then, the cooler on the output pipe of each storage container cools the mixed solution before entering the front-stage absorption tower for reaction, so that the low temperature of the reaction environment in each front-stage absorption tower is ensured, and the stability of sodium hypochlorite is ensured.
Drawings
Fig. 1 is a schematic diagram of a sodium hypochlorite continuous production device provided by the invention.
Detailed Description
The invention provides a sodium hypochlorite continuous production device, which comprises: n front-stage absorption towers, N storage containers corresponding to the N front-stage absorption towers one by one, a tail gas absorption tower T-03, a weak alkali storage tank V-03 and a mixer MX0, wherein N is larger than or equal to 1.
Output pipes are arranged on the storage container and the dilute alkali storage tank V-03, and a suction pump P0 and a cooler E0 are arranged on the output pipes. After the suction pump P0 is operated, the liquid in the corresponding storage container or the weak alkali storage tank can be sucked out, and the cooler E0 cools the passing liquid. In the present embodiment, the cooler E0 is a plate cooler, and other types of coolers may be used in specific implementations. And the input port of the cooler E0 is connected with the cooling water input device, and the output port of the cooler E0 is connected with the cooling water discharge device. Therefore, the cooling capacity compensation is carried out through the flowing of the cooling water, the liquid in the output pipe can be cooled in a heat exchange mode, and the low-temperature output of the liquid in the storage container or the dilute alkali storage tank is ensured.
The tail gas absorption tower T-03 is provided with a tail gas inlet, a tail gas discharge port, a light alkali inlet and a primary product discharge port, and the primary product discharge port, the tail gas inlet, the light alkali inlet and the tail gas discharge port are sequentially arranged from bottom to top. And each front section absorption tower is provided with a chlorine inlet, a chlorine outlet, a liquid inlet and a liquid outlet, wherein the liquid outlet, the chlorine inlet, the liquid inlet and the chlorine outlet are sequentially arranged from bottom to top. The N front-stage absorption towers are sequentially arranged, a chlorine inlet of the first front-stage absorption tower is connected with a chlorine supply device, chlorine inlets of the rest front-stage absorption towers are connected with a chlorine outlet of the front-stage absorption tower, and a chlorine outlet of the last front-stage absorption tower is connected with a tail gas inlet of a tail gas absorption tower T-03.
The input port of the mixer MX0 is used for inputting clear water and alkali liquor, and the output port of the mixer MX0 is communicated with the weak alkali storage tank V-03. Thus, the lye and water are mixed to form a weak base which is stored in a weak base storage tank. The alkali liquor inlet of the tail gas absorption tower T-03 is communicated with the output pipe of the light alkali storage tank V-03. The dilute alkali solution in the dilute alkali storage tank V-03 is cooled by a corresponding suction pump P0 through a corresponding cooler, and then enters the tail gas absorption tower T-03 through an output pipe to react with chlorine in the tower to obtain sodium hypochlorite, and unreacted gas is discharged from the high altitude through a tail gas discharge port of the tail gas absorption tower T-03. In the present embodiment, an exhaust pump C0 is attached to the exhaust port.
The primary product discharge port of the tail gas absorption tower T-03 is communicated with the last storage container, the liquid outlet of each front section absorption tower is communicated with the corresponding storage container, the output pipe of the Mth storage container is communicated with the liquid inlet of the Mth-1 front section absorption tower, M is more than or equal to 2 and less than or equal to N, the output pipe of the Nth storage container is also communicated with the liquid inlet of the Nth front section absorption tower, and the output pipe of the first front section absorption tower is connected to the secondary acid finished product tank V-04.
In this embodiment, a discharge valve is disposed at the liquid outlet of the last front-stage absorption tower. So, the mixed solution containing part of sodium hypochlorite in the tail gas absorption tower T-03 enters the last N storage container, then enters the N front-stage absorption tower in a state that the discharge valve is closed through the output pipe of the N storage container, after the solution in the N storage container is emptied, the discharge valve of the N front-stage absorption tower is opened, and the mixed solution which reacts with chlorine in the N front-stage absorption tower and has the sodium hypochlorite content increased is discharged into the N storage container; and then the mixed solution enters an N-1 pre-stage absorption tower through an output pipe of an N storage container to continuously react with chlorine so as to improve the content of sodium hypochlorite in the mixed solution. Similarly, the mixed solution sequentially passes through the M-th storage container, the M-1 th front-stage absorption tower … …, the second front-stage absorption tower, the second storage container and the first front-stage absorption tower, then enters the first storage container, and then enters the secondary acid finished product tank for storage after being cooled by the output pipe of the first storage container in the corresponding cooler.
In this embodiment, each front section absorption tower is provided with a packing layer, and the chlorine inlet and the liquid inlet are respectively located below and above the packing layer. Therefore, the filler layer can fully mix gas and liquid, the best absorption effect is achieved, and the chlorine utilization rate is improved. Similarly, a packing layer is arranged in the tail gas absorption tower T-03, and a tail gas inlet and a dilute alkali inlet are respectively positioned below and above the packing layer. The top of the storage container is provided with a tail gas outlet which is communicated with a tail gas inlet of the tail gas absorption tower T-03. And the secondary acid finished product tank V-04 is also provided with an exhaust outlet communicated with the exhaust inlet of the exhaust absorption tower T-03.
In this embodiment, the unreacted gas in each preceding-stage absorber enters the tail gas absorber T-03, and the gas in each storage container and the secondary acid product tank also enters the tail gas absorber. At least one tray is arranged above the packing layer in the tail gas absorption tower T-03, a light alkali inlet is arranged on the tail gas absorption tower T-03 corresponding to each tray, and a light alkali inlet is also arranged between the packing layer and the tray on the tail gas absorption tower T-03. Thus, the chlorine in the mixed gas in the tail gas absorption tower can be fully absorbed by the light alkali in the packing layer basically, and even if a small part of the chlorine passes through the packing layer, the chlorine can be fully mixed with the light alkali under the action of the tray to be absorbed. The arrangement of the tray avoids the unreacted chlorine contained in the tail gas.
In the concrete implementation, the liquid outlet of each front section absorption tower and the primary product discharge outlet of the tail gas absorption tower are provided with product on-line analysis meters so as to effectively control the secondary acid content in the liquid outlet of each section absorption tower and ensure the quality of secondary acid finished products.
The continuous sodium hypochlorite production device provided by the invention has the advantages that the chlorine flow direction is opposite to the weak alkali flow direction, and the chlorine and the weak alkali are in reverse contact. In this way, in the first front-stage absorption tower, the chlorine with highest purity reacts with the mixed solution with lowest alkali solution content, then the mixed gas with gradually reduced chlorine content contacts with the mixed solution with gradually increased alkali solution content, and finally in the tail gas absorption tower, the unreacted chlorine with extremely low content in the gas is directly mixed with light alkali. Thus, the absorption of chlorine is ensured, the cost is saved, and the pollution problem of tail gas emission is solved.
Example 1
Referring to fig. 1, the sodium hypochlorite continuous production apparatus provided in this embodiment includes two front-stage absorption towers, respectively referred to as a first-stage absorption tower T-01 and a second-stage absorption tower T-02, and storage containers corresponding to the first-stage absorption tower T-01 and the second-stage absorption tower T-02 are respectively referred to as a final product storage tank V-01 and a semi-final product storage tank V-02.
The chlorine inlet of the first-stage absorption tower T-01 is connected with a chlorine supply device, the chlorine outlet of the first-stage absorption tower T-01 is communicated with the chlorine inlet of the second-stage absorption tower T-02, and the chlorine outlet of the second-stage absorption tower T-02 is communicated with the tail gas inlet. The output pipe of the dilute alkali storage tank V-03 is communicated with the dilute alkali inlet of the tail gas absorption tower T-03, and the primary product discharge port of the tail gas absorption tower T-03 and the liquid outlet of the secondary absorption tower T-02 are both communicated with the semi-finished product storage tank V-02. The output pipe of the semi-finished product storage tank V-02 is respectively communicated with the liquid inlet of the first section of absorption tower T-01 and the liquid inlet of the second section of absorption tower T-02. The liquid outlet of the second section of absorption tower T-02 is communicated with the semi-finished product storage tank V-02, and the liquid outlet of the first section of absorption tower T-01 is communicated with the finished product storage tank V-01. The output pipe of the finished product storage tank V-01 is communicated with the secondary acid finished product tank V-04.
The top of the semi-finished product storage tank V-02 and the top of the finished product storage tank V-01 are respectively provided with an exhaust outlet and are respectively communicated with the tail gas inlet of the tail gas absorption tower T-03. In the embodiment, alkali liquor and water form light alkali through a mixer MX0 and enter a light alkali storage tank, and the light alkali in the light alkali storage tank enters a tail gas absorption tower through an output pipe through a cooler under the action of a suction pump; the light alkali in the tail gas absorption tower reacts with chlorine to generate sodium hypochlorite and tail gas, the unreacted gas phase is led out from a blower to be vented at high position, and the mixed solution of sodium hypochlorite and residual light alkali enters a semi-finished product storage tank; the mixed solution in the semi-finished product storage tank enters a first-stage absorption tower and a second-stage absorption tower through a suction pump and a cooler corresponding to the semi-finished product storage tank; chlorine in the second-stage absorption tower reacts with alkali liquor in the mixed solution to generate sodium hypochlorite, and then the mixed solution in the second-stage absorption tower returns to a semi-finished product storage tank; through the circulation of the two-stage absorption tower, the content of the hypochlorous acid and alkali in the semi-finished product storage tank is increased, and the alkali liquor is reduced; in the first-stage absorption tower, chlorine reacts with the rest alkali liquor in the mixed solution to obtain a mixed solution with sodium hypochlorite content reaching the standard, and the mixed solution is sent to a finished product storage tank; and outputting and storing the sodium hypochlorite solution in the finished product storage tank through a corresponding suction pump and a cooler.
The residual gas in the first-stage absorption tower enters the tail gas absorption tower through the second-stage absorption tower, the residual gas in the second-stage absorption tower enters the tail gas absorption tower, and the gas in the tail gas absorption tower is subjected to light alkali absorption treatment on a tray and then is discharged at a high position under the action of an exhaust pump C0.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (10)
1. A sodium hypochlorite continuous production device, comprising: n front-stage absorption towers, N storage containers corresponding to the N front-stage absorption towers one by one, a tail gas absorption tower (T-03) and a weak alkali storage tank (V-03), wherein N is not less than 2;
output pipes are arranged on the storage container and the dilute alkali storage tank (V-03), and a suction pump (P0) and a cooler (E0) are arranged on the output pipes;
a tail gas inlet, a tail gas discharge port, a light alkali inlet and a primary product discharge port are arranged on the tail gas absorption tower (T-03), and the primary product discharge port, the tail gas inlet, the light alkali inlet and the tail gas discharge port are sequentially arranged from bottom to top; each front section absorption tower is provided with a chlorine inlet, a chlorine outlet, a liquid inlet and a liquid outlet, wherein the liquid outlet, the chlorine inlet, the liquid inlet and the chlorine outlet are sequentially arranged from bottom to top;
the N front-stage absorption towers are sequentially arranged, a chlorine inlet of the first front-stage absorption tower is connected with a chlorine supply device, chlorine inlets of the rest front-stage absorption towers are all connected with a chlorine outlet of the front-stage absorption tower, and a chlorine outlet of the last front-stage absorption tower is connected with a tail gas inlet of a tail gas absorption tower (T-03); the alkali liquor inlet of the tail gas absorption tower (T-03) is communicated with the output pipe of the light alkali storage tank (V-03); the primary product discharge port of the tail gas absorption tower (T-03) is communicated with the last storage container, the liquid outlet of each front-stage absorption tower is communicated with the corresponding storage container, the output pipe of the Mth storage container is communicated with the liquid inlet of the Mth-1 front-stage absorption tower, M=N is more than or equal to 2, the output pipe of the Nth storage container is also communicated with the liquid inlet of the Nth front-stage absorption tower, and the output pipe of the first front-stage absorption tower is connected to a secondary acid finished product tank (V-04);
the top of the storage container is provided with a tail gas outlet which is communicated with a tail gas inlet of a tail gas absorption tower (T-03);
and finally, in an absorption tower, unreacted chlorine with extremely low content in the gas is directly mixed with light alkali.
2. The apparatus for continuously producing sodium hypochlorite as claimed in claim 1, wherein a discharge valve is provided at the liquid outlet of the last preceding absorption tower.
3. The continuous sodium hypochlorite production device as claimed in claim 1, wherein each front-stage absorption tower is internally provided with a packing layer, and the chlorine inlet and the liquid inlet are respectively positioned below and above the packing layer.
4. The sodium hypochlorite continuous production device as claimed in claim 1, wherein a filler layer is arranged in the tail gas absorption tower (T-03), and the tail gas inlet and the light alkali inlet are respectively positioned below and above the filler layer.
5. The sodium hypochlorite continuous production device as claimed in claim 4, wherein at least one tray is arranged above the packing layer in the tail gas absorption tower (T-03), a light alkali inlet is arranged on each tray on the tail gas absorption tower (T-03), and a light alkali inlet is also arranged between the packing layer and the tray on the tail gas absorption tower (T-03).
6. The sodium hypochlorite continuous production device as claimed in claim 1, wherein the secondary acid product tank (V-04) is also provided with an exhaust gas outlet communicated with the exhaust gas inlet of the exhaust gas absorption tower (T-03).
7. The apparatus for continuously producing sodium hypochlorite as claimed in claim 1, wherein an exhaust pump (C0) is installed at the exhaust port.
8. The sodium hypochlorite continuous production device as claimed in claim 1, wherein the cooler (E0) is a plate cooler, and the inlet of the cooler (E0) is connected with the cooling water input device, and the outlet of the cooler (E0) is connected with the cooling water discharge device.
9. The sodium hypochlorite continuous production device as claimed in claim 1, further comprising a mixer (MX 0), wherein the input of the mixer (MX 0) is used for inputting the fresh water and the alkali liquor, and the output thereof is connected to the weak alkali storage tank (V-03).
10. Continuous production plant of sodium hypochlorite as claimed in any one of claims 1 to 9, characterized in that it comprises two front-stage absorption towers, respectively called primary absorption tower (T-01) and secondary absorption tower (T-02), and the storage containers corresponding to the primary absorption tower (T-01) and the secondary absorption tower (T-02) are respectively called finished product storage tank (V-01) and semi-finished product storage tank (V-02); the chlorine inlet of the first-stage absorption tower (T-01) is connected with a chlorine supply device, the chlorine outlet of the first-stage absorption tower (T-01) is communicated with the chlorine inlet of the second-stage absorption tower (T-02), and the chlorine outlet of the second-stage absorption tower (T-02) is communicated with a tail gas inlet; the output pipe of the dilute alkali storage tank (V-03) is communicated with the dilute alkali inlet of the tail gas absorption tower (T-03), and the primary product discharge port of the tail gas absorption tower (T-03) and the liquid outlet of the second-stage absorption tower (T-02) are both communicated with the semi-finished product storage tank (V-02); the output pipe of the semi-finished product storage tank (V-02) is respectively communicated with the liquid inlet of the first section of absorption tower (T-01) and the liquid inlet of the second section of absorption tower (T-02); the liquid outlet of the second section of absorption tower (T-02) is communicated with a semi-finished product storage tank (V-02), and the liquid outlet of the first section of absorption tower (T-01) is communicated with a finished product storage tank (V-01); the output pipe of the finished product storage tank (V-01) is communicated with the secondary acid finished product tank;
the top of the semi-finished product storage tank (V-02) and the top of the finished product storage tank (V-01) are respectively provided with an exhaust outlet and are respectively communicated with the tail gas inlet of the tail gas absorption tower (T-03).
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| CN107010599A (en) | 2017-08-04 |
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