CN201848198U - Industrial waste gas treatment and salt regenerating unit - Google Patents
Industrial waste gas treatment and salt regenerating unit Download PDFInfo
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- CN201848198U CN201848198U CN2010202549044U CN201020254904U CN201848198U CN 201848198 U CN201848198 U CN 201848198U CN 2010202549044 U CN2010202549044 U CN 2010202549044U CN 201020254904 U CN201020254904 U CN 201020254904U CN 201848198 U CN201848198 U CN 201848198U
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Abstract
The utility model discloses an industrial waste gas treatment and salt regenerating unit comprising a waste gas treatment device, a neutralization deslagging device, a basic solution concentration device, a water main, an alkali liquor supplying tank and a hydrochloric acid storage tank, wherein the waste gas treatment device is provided with absorption towers from number one to number five, a gas-liquid separator, a mixer, an acid liquor clarification tank and an alkali liquor transfer tank; the neutralization deslagging device is provided with a neutralization stirred tank, a purification tank, a pressure filter and a basic solution transfer tank; and the basic solution concentration device is provided with a preheater, a heater, an evaporator, a crystallizer, a basic solution stirring tank, a centrifugal machine, a condenser and a condensation water tank. The system can effectively treat the industrial waste gas containing chlorine and hydrogen chloride gases, as the system recovers products from the waste liquor, the additional value of the system is improved, and the problem of sewage discharge can be avoided.
Description
Technical field
The utility model relates to industrial waste gas to be handled and the salt regenerating unit.
Background technology
The industrial waste gas that contains chlorine and hydrogen chloride gas that produces in the industrial production need be through handling, and could discharge after up to standard.China Patent No. is that 200720005231.7 utility model patent specification discloses a kind of emission-control equipment, have one-level scrubbing tower, secondary turbulent tower and three grades of turbulent towers, one-level scrubbing tower and two, three grades of turbulent towers are equipped with heat exchanger respectively one, two, No. three, and native system also has supply mains in alkali lye house steward, water inlet pipe, the cooling, cooling backwater house steward, discharge manifold in addition.Waste gas enters the one-level scrubbing tower by the blower fan traction, and the water with the contrary spray of shower nozzle in the rapid washing pipe of one-level scrubbing tower fully contacts with hydrogen chloride gas, and hydrogen chloride is after the one-level washing, and chlorine gas concentration also decreases, and enters the secondary turbulent tower again.Hydrogen chloride gas is further absorbed, and chlorine gas concentration also further reduces, and waste gas enters in three grades of turbulent towers, mainly handles chlorine.Waste gas is discharged by blower fan after three grades of absorptions.When circulation fluid is that concentration of hydrochloric acid in the absorption liquid acquires a certain degree, absorption liquid enters acid accumulator settling basin by the recycling carrier pipe.Though above-mentioned emission-control equipment is handled the industrial waste gas that contains chlorine and hydrogen chloride gas, make the gas of discharge up to standard, if relief liquor is not handled, still there is pollution problem.
Summary of the invention
The purpose of this utility model is to propose to carry out the industrial waste gas that contains chlorine and hydrogen chloride gas a kind of industrial waste gas processing and the salt regenerating unit of pollution-free processing and energy output Nacl.
For achieving the above object, the utility model is taked following technical scheme:
The utility model comprise emission-control equipment, water main, alkali lye for groove, salt acid storage tank and in and deslagging device and saline solution enrichment facility;
Described emission-control equipment has turn trough in 1 to No. 5 absorption tower, gas-liquid separator, blender and acid accumulator settling basin and the alkali lye; Industrial waste gas is discharged by blower fan behind gas-liquid separator through 1 to No. 5 absorption tower successively again; Described blender is accepted respectively from water main and alkali lye neutral water and the alkali lye for groove, the liquid outlet of blender is connected with the inlet on No. 5 absorption towers and No. 4 absorption towers respectively, the liquid outlet of aerosol separator is connected with the liquid mouth that returns on No. 5 absorption towers, the overfall on No. 5 absorption towers is connected with the fluid infusion mouth on No. 4 absorption towers, the overfall on No. 4 absorption towers is connected with the fluid infusion mouth on No. 3 absorption towers, and each leakage fluid dram on above-mentioned No. 3 absorption towers, No. 4 absorption towers and No. 5 absorption towers all is connected with turn trough in the described alkali lye; The neutral water from the water main is accepted on described No. 2 absorption towers, and the overfall on No. 2 absorption towers is connected with the fluid infusion mouth on No. 1 absorption tower, and the leakage fluid dram on No. 1 absorption tower and No. 2 absorption towers all is connected with described acid accumulator settling basin; The upper and lower part of described acid accumulator settling basin has clear liquid delivery outlet and suspension outlet respectively, and a wherein clear liquid delivery outlet of acid accumulator settling basin is connected with described salt acid storage tank;
In described and deslagging device have in and turn trough in stirred tank, deblending slot, filter press and the saline solution; In described and stirred tank accept alkali lye from turn trough in the hydrochloric acid of described acid accumulator settling basin and the described alkali lye, described deblending slot is accepted the suspension from described acid accumulator settling basin, all be connected with described filter press with the liquid outlet of stirred tank and the discharging opening of deblending slot in described, the filter liquor of filter press is pumped into turn trough in the described saline solution;
Described saline solution enrichment facility has preheater, heater, evaporimeter, crystallizer, saline solution tank diameter, centrifuge, condenser and condensate draining, in described with the saline solution of deslagging device in the infusion port of turn trough be connected with the inlet of described preheater, the liquid outlet of preheater is connected with the charging aperture of described heater, the discharging opening of evaporimeter is connected with the charging aperture of described crystallizer, the discharging of crystallizer is imported described centrifuge through the saline solution tank diameter, the liquid phase of centrifuge drains in the filtrate storage tank, and the solid phase of centrifuge is dense salt; The condensed water that condenser produces is collected by the condensed water storage tank.
No. 1 absorption tower of described emission-control equipment is a spray absorber, No. 2 absorption towers and No. 3 absorption towers are that rapids is towards spray absorber, No. 4 absorption towers and No. 5 absorption towers are packed absorber, be connected by circulation pipe between the liquid outlet on each absorption tower and the shower nozzle, be serially connected with water pump in each circulation pipe, absorption liquid forms circulation; Also be serially connected with heat exchanger in each circulation pipe on described No. 1 absorption tower, No. 2 absorption towers, No. 3 absorption towers.
Be provided with the saline solution tank diameter in described and in the filter press of deslagging device and the saline solution between the turn trough.
Described saline solution enrichment facility also has rinsing bowl, is connected serial connection washing pump in the circulation pipe between the upper and lower Butterworth Hatch of heater and the rinsing bowl by circulation pipe.
The utlity model has following good effect: the utlity model has emission-control equipment, in and deslagging device and saline solution enrichment facility, emission-control equipment adopts the Pyatyi absorption tower that waste gas is handled, and the Pyatyi absorption tower adopts fountain, rapids towards three types of fountain and material filling types, the absorption liquid that the two-stage absorption tower is used before in the Pyatyi absorption tower is a neutral water, the absorption liquid that three grades of absorption towers, back are used is an alkali lye, so waste gas is being absorbed fully through chlorine behind each absorption tower, but also helps hydrochloric acid is collected.Handle with deslagging device and saline solution enrichment facility in the waste liquid warp that in waste gas treatment process, produces, therefrom reclaim salt acid product and Nacl product.Native system can be administered the industrial waste gas that contains chlorine and hydrogen chloride gas effectively, owing to from waste liquid, reclaim product, thereby improve the added value of native system, there is not simultaneously the sewage discharge problem, have in the absorption tower of native system and adopt fluid infusion step by step, utilize again, for example steam reuse after becoming condensed water at the relief liquor on each link or after recycling or collecting, the parting liquid of aerosol separator adds in the absorption tower and utilizes, so energy-conservation.
Description of drawings
For the easier quilt of content of the present utility model is clearly understood, according to specific embodiment also in conjunction with the accompanying drawings, the utility model is described in further detail, wherein below
Fig. 1 is the utility model embodiment diagrammatic sketch;
Fig. 2 be in and another embodiment diagrammatic sketch of deslagging device.
The specific embodiment
See Fig. 1, present embodiment comprise emission-control equipment A, in and deslagging device B, saline solution enrichment facility C and water main 1, alkali lye for groove 2, salt acid storage tank 3, water leg 4 and filtrate storage tank 5.Water main 1 neutral water is provided jointly by the water for industrial use of outside and the condensed water of native system generation.
Described emission-control equipment A has turn trough A10 in No. 1 absorption tower A1, No. 2 absorption tower A2, No. 3 absorption tower A3, No. 4 absorption tower A4, No. 5 absorption tower A5, aerosol separator A6, blender A7 and acid accumulator settling basin A9 and the alkali lye.Above-mentioned No. 1 absorption tower A1 is a spray absorber, and No. 2 absorption tower A2 and No. 3 absorption tower A3 are that rapids is towards spray absorber.No. 4 absorption tower A4 and No. 5 absorption tower A5 are packed absorber.Top in the spray absorber is provided with spray head.Rapids is provided with spray head towards the top in the spray absorber, is provided with rapids in the rapid washing pipe towards shower nozzle.Top in the packed absorber is provided with spray head, has filler in the tower.Be connected by circulation pipe between the liquid outlet on each absorption tower and the shower nozzle, be serially connected with water pump a in each circulation pipe, the absorption liquid of each tower forms circulation.Because handle in the waste gas process and can produce exothermic reaction, the absorption efficiency of tower descends under hot conditions, is serially connected with heat exchanger d in each circulation pipe of No. 1 absorption tower A1, No. 2 absorption tower A2, No. 3 absorption tower A3, reduces the temperature of absorption liquid.
Be connected by pipe A11 between the air inlet of the exhaust outlet of No. 1 absorption tower A1 and No. 2 absorption tower A2, be connected by pipe A12 between the air inlet of the exhaust outlet of No. 2 absorption tower A2 and No. 3 absorption tower A3, be connected by pipe A13 between the exhaust outlet of No. 3 absorption tower A3 and No. 4 absorption tower A4 air inlets, be connected by pipe A14 between the air inlet of the exhaust outlet of No. 4 absorption tower A4 and No. 5 absorption tower A5, be connected by pipe A15 between the air inlet of the exhaust outlet on No. 5 absorption towers and aerosol separator A6, the gas outlet of aerosol separator A6 connects delivery pipe A16, serial connection blower fan A8 among the delivery pipe A16, industrial waste gas is discharged by blower fan A8 behind aerosol separator A6 through 1 to No. 5 absorption tower successively again.
Water main 1 and alkali lye are connected with the feed tube of described blender A7 for managing 21 by the first water supply arm 11 and alkali lye respectively for groove 2; Water supply arm 11 and alkali lye is for respectively installing flowmeter e on the pipe 21, is used to control the neutral water that enters blender A7 and the ratio of alkali lye.The liquid outlet of blender A7 is connected with the inlet of No. 5 absorption tower A5, is connected with the inlet of No. 4 absorption tower A4 by pipe A27 by pipe A26, the liquid outlet of aerosol separator A6 is connected with the liquid mouth that returns of No. 5 absorption tower A5 by pipe A25, and the parting liquid of aerosol separator A6 adds among No. 5 absorption tower A5 and utilizes.The overfall of No. 5 absorption tower A5 is connected with the fluid infusion mouth of No. 4 absorption tower A4 by pipe A24, the overfall of No. 4 absorption tower A4 is connected with the fluid infusion mouth of No. 3 absorption tower A3 by pipe A23, each leakage fluid dram of the leakage fluid dram of the leakage fluid dram of No. 3 absorption tower A3, No. 4 absorption tower A4 and No. 5 absorption tower A5 is connected with alkali lye discharge manifold A28 by delivery pipe, and alkali lye discharge manifold A28 is connected with turn trough A10 in the described alkali lye.Water main 1 second arm 12 is connected with the water inlet of No. 2 absorption tower A2, be connected by pipe A22 between the fluid infusion mouth of the overfall of No. 2 absorption tower A2 and No. 1 absorption tower A1, the leakage fluid dram of the leakage fluid dram of No. 1 absorption tower A1 and No. 2 absorption tower A2 respectively is connected with acid solution discharge manifold A21 by discharging tube, and acid solution discharge manifold 21 is connected with described acid accumulator settling basin A9.The upper and lower part of described acid accumulator settling basin A9 has clear liquid delivery outlet and suspension outlet respectively, the wherein clear liquid delivery outlet of acid accumulator settling basin A9 is connected with described salt acid storage tank 3 by pipe A29, the clear liquid on acid accumulator settling basin A9 top promptly is a watery hydrochloric acid, delivers to clear liquid in the salt acid storage tank 3 then as reclaiming product.The fluid infusion mode on above-mentioned No. 1 absorption tower, No. 3 absorption towers, No. 4 absorption towers is all by the overflow supply of first grade absorption tower afterwards, absorption liquid when No. 1 absorption tower and No. 2 absorption towers reaches finite concentration, then drive valve and enter acid accumulator settling basin A9, absorption liquid when No. 3 absorption towers, No. 4 absorption towers and No. 5 absorption towers reaches finite concentration, then drives valve and enters turn trough A10 in the alkali lye.
Above-mentioned water main's 1 second arm 12 is connected except the water inlet with No. 2 absorption tower A2, and also the water inlet with No. 3 absorption tower A3 is connected, and water for cleaning is provided.
In described and deslagging device B have in and turn trough B4 in stirred tank B1, deblending slot B2, filter press B3 and the saline solution.Be added with reagent in the deblending slot.Be connected with the liquid outlet of turn trough A10 in the alkali lye with the clear liquid delivery outlet of described acid accumulator settling basin A9 with pipe B7 by pipe B6 respectively with two input ports of stirred tank B1 in described, the charging aperture of described deblending slot B2 is connected with the suspension outlet of described acid accumulator settling basin A9 by pipe B8, the suspension pump of acid accumulator settling basin A9 is delivered to deblending slot B2, in with the discharging opening of the liquid outlet of stirred tank B1 and deblending slot B2 respectively by pipe B9 with manage B10 and be connected with described filter press B3, come the rare saline solution of self-neutralization stirred tank B1 and the suspension of deblending slot B2 to pass through filter press B3 simultaneously, obtain filter residue and filter liquor, rare saline solution is subjected to the effect of reagent in the filter process of filter press B3, foreign ion obtains removing, filter liquor is that the purity of rare saline solution is improved, and the filter liquor of filter press B3 is pumped into turn trough B4 in the described saline solution.
Described saline solution enrichment facility C has preheater C1, heater C2, evaporimeter C3, crystallizer C4, dense saline solution tank diameter C5, centrifuge C6, condenser C7 and condensate draining C8.Be provided with circulation pipe between described crystallizer C4 and the heater C2, be serially connected with circulating pump C11 in the circulation pipe.Be connected by pipe C12 between the inlet of the infusion port of turn trough B4 and described preheater C1 in described and in the saline solution of deslagging device B, be connected by pipe C13 between the charging aperture of the liquid outlet of preheater C1 and described heater C2, be connected by pipe C14 between the charging aperture of the discharging opening of evaporimeter C3 and described crystallizer C4, is connected by pipe C15 between the discharging opening of crystallizer C4 and the described dense saline solution tank diameter C5, is connected by managing C16 between the charging aperture of dense saline solution tank diameter C5 and described centrifuge C6.
Rare saline solution of turn trough B4 output is pumped in the preheater C1 by pipe C12 in the saline solution, deliver to heater C2 heating through preheating after manage C13, and successively through pipe C14, evaporimeter C3, crystallizer C4, owing between crystallizer C4, heater C2 and the evaporimeter C3 closed circuit is arranged, rare saline solution progressively concentrates, and concentrate is pumped to saline solution tank diameter C5 by pipe C15, deliver to centrifuge C6 by pipe C16 again and carry out liquid, solid phase separation, liquid phase is discharged in the filtrate storage tank 5, can reuse, and solid phase is Nacl.
Give birth to steam and enter heater C2, a secondary steam part enters preheater C1 by pipe C18, all the other secondary steams enter condenser C7 by pipe C14, evaporimeter C3, pipe C17 successively, the condensation flow that condenser C7 produces is to condensed water storage tank C8, the condensed water that condensed water among the condensed water storage tank C8 and preheater C1 produce respectively by manage 20 and pipe 19 be pooled in the water leg 4, the water of water leg 4 offers water main 1.
Described saline solution enrichment facility C also has rinsing bowl C9, is connected serial connection washing pump C10 in the circulation pipe between the upper and lower Butterworth Hatch of heater C2 and the rinsing bowl C9 by circulation pipe.
The body of the tower bottom on above-mentioned each absorption tower is equipped with thermometer t that detects the absorption liquid temperature and the densimeter i that detects absorption liquid concentration.In addition, about the position is provided with liquid level gauge and pH meter, be provided with corresponding valve in the pipeline.
During shown in Figure 2 is and another embodiment of deslagging device, in and be provided with the saline solution tank diameter B5 that has agitator between the filter press B3 of deslagging device B and the saline solution lead-over groove B4.
Claims (4)
1. an industrial waste gas is handled and the salt regenerating unit, comprises that emission-control equipment (A) and water main (1), alkali lye are for groove (2) and salt acid storage tank (3); It is characterized in that: during native system also comprises and deslagging device (B), saline solution enrichment facility (C);
Described emission-control equipment (A) has turn trough (A10) in 1 to No. 5 absorption tower, gas-liquid separator (A6), blender (A7) and acid accumulator settling basin (A9) and the alkali lye; Industrial waste gas is discharged by blower fan (A8) behind gas-liquid separator (A6) through 1 to No. 5 absorption tower successively again; Described blender (A7) is accepted respectively neutral water and the alkali lye from water main (1) and alkali lye confession groove (2), the liquid outlet of blender (A7) is connected with the inlet of No. 5 absorption towers (A5) with No. 4 absorption towers (A4) respectively, the liquid outlet of aerosol separator (A6) is connected with the liquid mouth that returns on No. 5 absorption towers (A5), the overfall on No. 5 absorption towers (A5) is connected with the fluid infusion mouth on No. 4 absorption towers (A4), the overfall on No. 4 absorption towers (A4) is connected with the fluid infusion mouth on No. 3 absorption towers (A3), above-mentioned No. 3 absorption towers (A3), each leakage fluid dram on No. 4 absorption towers (A4) and No. 5 absorption towers (A5) all is connected with turn trough (A10) in the described alkali lye; The neutral water from water main (1) is accepted on described No. 2 absorption towers (A2), the overfall on No. 2 absorption towers (A2) is connected with the fluid infusion mouth on No. 1 absorption tower (A1), and the leakage fluid dram on No. 1 absorption tower (A1) and No. 2 absorption towers (A2) all is connected with described acid accumulator settling basin (A9); The upper and lower part of described acid accumulator settling basin (A9) has clear liquid delivery outlet and suspension outlet respectively, and a wherein clear liquid delivery outlet of acid accumulator settling basin (A9) is connected with described salt acid storage tank (3);
In described and deslagging device (B) have in and turn trough (B4) in stirred tank (B1), deblending slot (B2), filter press (B3) and the saline solution; In described and stirred tank (B1) accept alkali lye from turn trough (A10) in the hydrochloric acid of described acid accumulator settling basin (A9) and the described alkali lye, described deblending slot (B2) is accepted the suspension from described acid accumulator settling basin (A9), all be connected with described filter press (B3) with the liquid outlet of stirred tank (B1) and the discharging opening of deblending slot (B2) in described, the filter liquor of filter press (B3) is pumped into turn trough in the described saline solution (B4);
Described saline solution enrichment facility (C) has preheater (C1), heater (C2), evaporimeter (C3), crystallizer (C4), saline solution tank diameter (C5), centrifuge (C6), condenser (C7) and condensate draining (C8), in described with the saline solution of deslagging device (B) in the infusion port of turn trough (B4) be connected with the inlet of described preheater (C1), the liquid outlet of preheater (C1) is connected with the charging aperture of described heater (C2), the discharging opening of evaporimeter (C3) is connected with the charging aperture of described crystallizer (C4), the discharging of crystallizer (C4) is imported described centrifuge (C6) through saline solution tank diameter (C5), the liquid phase of centrifuge (C6) drains in the filtrate storage tank (5), and the solid phase of centrifuge (C6) is dense salt; The condensed water that condenser (C7) produces is collected by condensed water storage tank (C8).
2. a kind of industrial waste gas according to claim 1 is handled and the salt regenerating unit, it is characterized in that: No. 1 absorption tower (A1) of described emission-control equipment is spray absorber, No. 2 absorption towers (A2) and No. 3 absorption towers (A3) are that rapids is towards spray absorber, No. 4 absorption towers (A4) and No. 5 absorption towers (A5) are packed absorber, be connected by circulation pipe between the liquid outlet on each absorption tower and the shower nozzle, be serially connected with water pump (a) in each circulation pipe, absorption liquid forms circulation; Also be serially connected with heat exchanger (d) in each circulation pipe on described No. 1 absorption tower (A1), No. 2 absorption towers (A2), No. 3 absorption towers (A3).
3. industrial waste gas according to claim 1 is handled and the salt regenerating unit, it is characterized in that: be provided with saline solution tank diameter (B5) between the turn trough (B4) in described and in the filter press (B3) of deslagging device (B) and the saline solution.
4. a kind of industrial waste gas according to claim 1 is handled and the salt regenerating unit, it is characterized in that: described saline solution enrichment facility (C) also has rinsing bowl (C9), be connected serial connection washing pump (C10) in the circulation pipe between the upper and lower Butterworth Hatch of heater (C2) and the rinsing bowl (C9) by circulation pipe.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202549044U CN201848198U (en) | 2010-07-12 | 2010-07-12 | Industrial waste gas treatment and salt regenerating unit |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202549044U CN201848198U (en) | 2010-07-12 | 2010-07-12 | Industrial waste gas treatment and salt regenerating unit |
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| CN201848198U true CN201848198U (en) | 2011-06-01 |
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| CN2010202549044U Expired - Lifetime CN201848198U (en) | 2010-07-12 | 2010-07-12 | Industrial waste gas treatment and salt regenerating unit |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101862586A (en) * | 2010-07-12 | 2010-10-20 | 江苏海鹏防腐设备有限公司 | System for industrial waste gas treatment and salt regeneration |
| CN111116523A (en) * | 2019-12-30 | 2020-05-08 | 浙江新和成股份有限公司 | System and process for producing α -chloro- α -acetyl-gamma-butyrolactone |
| CN114950078A (en) * | 2022-06-14 | 2022-08-30 | 扬州联博药业有限公司 | Waste gas treatment process in doxycycline hydrochloride production |
-
2010
- 2010-07-12 CN CN2010202549044U patent/CN201848198U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101862586A (en) * | 2010-07-12 | 2010-10-20 | 江苏海鹏防腐设备有限公司 | System for industrial waste gas treatment and salt regeneration |
| CN101862586B (en) * | 2010-07-12 | 2012-03-07 | 江苏海鹏防腐设备有限公司 | System for industrial waste gas treatment and salt regeneration |
| CN111116523A (en) * | 2019-12-30 | 2020-05-08 | 浙江新和成股份有限公司 | System and process for producing α -chloro- α -acetyl-gamma-butyrolactone |
| CN111116523B (en) * | 2019-12-30 | 2021-09-07 | 浙江新和成股份有限公司 | System and process for producing alpha-chloro-alpha-acetyl-gamma-butyrolactone |
| CN114950078A (en) * | 2022-06-14 | 2022-08-30 | 扬州联博药业有限公司 | Waste gas treatment process in doxycycline hydrochloride production |
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Granted publication date: 20110601 Effective date of abandoning: 20120502 |