CN111495123A - Antioxidant tail gas recovery processing system - Google Patents
Antioxidant tail gas recovery processing system Download PDFInfo
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- CN111495123A CN111495123A CN202010394023.0A CN202010394023A CN111495123A CN 111495123 A CN111495123 A CN 111495123A CN 202010394023 A CN202010394023 A CN 202010394023A CN 111495123 A CN111495123 A CN 111495123A
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1412—Controlling the absorption process
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- C01B7/00—Halogens; Halogen acids
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Abstract
The invention discloses an antioxidant tail gas recovery processing system, which comprises a comprehensive absorption tower, a finished hydrochloric acid tank, a vacuum unit and an alkali liquor preparation tank; the comprehensive absorption tower comprises a finished product liquid intermediate tank, a primary absorption section metal cylinder, a gas-liquid collector, a secondary absorption section metal cylinder, a gas-liquid mixer, a gas-liquid mixing chamber and a tertiary absorption tower which are sequentially connected from bottom to top; the method can recycle the byproduct hydrogen chloride gas to prepare hydrochloric acid, thereby changing waste into valuable; meanwhile, the reaction pressure in the preparation process of the antioxidant 168 is controlled, so that the control of the generation speed of hydrogen chloride gas and the effective control of the reaction speed in the preparation process of the antioxidant 168 are realized through the control of the reaction pressure, and the product quality of the antioxidant 168 is improved; in addition, the system has the characteristics of compact structure, small duty, low investment cost, simple operation, low running cost, free switching between the pressure system and the absorbent system and easy standard reaching of tail gas emission.
Description
Technical Field
The invention relates to a tail gas treatment system, in particular to an antioxidant 168 tail gas recovery system.
Background
The antioxidant 168 is a phosphite antioxidant with excellent performance, is an indispensable heat stabilizer in resin processing, can effectively prevent the generation of hydrogen halide in the processing process, thereby greatly reducing the corrosion to a mold, and can decompose hydroperoxide formed in the degradation of a polymer to play a good role in synergism. Is one of the phosphite ester auxiliary antioxidants which are commonly used internationally at present, has good hydrolysis resistance, high temperature resistance, small volatility and strong extraction resistance, and can obviously improve the light stability of products. Meanwhile, the antioxidant 168 is also a relatively safe heat-stable additive at present, is approved by the FDA in the United states, is approved by countries such as Germany, Switzerland, Japan, Italy and the like to be used in food contact products, has wide application and has good development prospect. The domestic market demand is about 1400-1600 t/a and is increasing. At present, more than 10 units are used for researching and producing antioxidant 168 products in China, but most of the units have small scale and low yield, and particularly the problem of tail gas recovery of byproduct hydrogen chloride is not solved.
The solubility of hydrogen chloride in water is considerable (1: 450); the technology for producing hydrochloric acid by absorbing hydrogen chloride with water is mature and is the most conventional treatment method for industrial byproduct hydrogen chloride. The most complete hydrogen chloride absorption and tail gas treatment process system at the present stage comprises: a comprehensive absorption system consisting of a first-stage falling film absorber, a second-stage falling film absorber, a third-stage tail gas absorption tower, a fourth-stage water conservancy injection pump and a fifth-stage alkaline washing tower; has strong absorption capacity; thorough tail gas treatment and the like. The disadvantages are that: the system device is large; the one-time investment and the operation cost are high.
In real production, because the system is not generally the main process route; in order to save investment and reduce later operation cost; few enterprises build complete systems sets. In particular to a process device with small production scale and unstable hydrogen chloride yield; on the premise of meeting the process requirements, users put forward higher requirements on the aspects of one-time investment, occupied space, running cost, simple and convenient operation degree and the like; the demand and the expectation on the single-machine equipment with integrated design are high.
Disclosure of Invention
The invention aims to provide a tail gas recovery processing system in the production and preparation process of an antioxidant 168. The byproduct hydrogen chloride gas is recycled to prepare hydrochloric acid, so that waste is changed into valuable; meanwhile, the reaction pressure in the preparation process of the antioxidant 168 is controlled, so that the control of the generation speed of hydrogen chloride gas and the effective control of the reaction speed in the preparation process of the antioxidant 168 are realized through the control of the reaction pressure, and the product quality of the antioxidant 168 is improved; in addition, the system has the characteristics of compact structure, small duty, low investment cost, simple operation, low running cost, free switching between the pressure system and the absorbent system and easy standard reaching of tail gas emission.
The technical scheme of the invention is as follows: the antioxidant tail gas recovery treatment system comprises a comprehensive absorption tower, a finished hydrochloric acid tank, a vacuum unit and an alkali liquor preparation tank;
the comprehensive absorption tower comprises a finished product liquid intermediate tank, a primary absorption section metal cylinder, a gas-liquid collector, a secondary absorption section metal cylinder, a gas-liquid mixer, a gas-liquid mixing chamber and a tertiary absorption tower which are sequentially connected from bottom to top;
the bottom of finished product liquid intermediate tank is equipped with absorption liquid circulation export and finished product liquid export, the finished product liquid export through first pipeline with the finished product hydrochloric acid jar is connected, is equipped with the concentrated hydrochloric acid pump on the first pipeline, and the middle part is equipped with the absorption liquid import, and upper portion is equipped with first hydrogen chloride gas import, and first hydrogen chloride gas import and antioxidant tail gas export are through ninth pipe connection, are equipped with pressure regulating valve on the ninth pipeline.
A first floating tube plate is arranged inside the joint of the primary absorption section metal cylinder and the finished product liquid intermediate tank, a first graphite heat exchange tube is connected in an overflowing hole of the first floating tube plate, a first circulating water inlet and a first sewage discharge outlet are arranged at the lower end of the primary absorption section metal cylinder, and a first vent outlet and a first circulating water outlet are arranged at the upper end of the primary absorption section metal cylinder;
the gas-liquid collector is connected with the primary absorption section metal cylinder through a first fixed tube plate, the lower side of an overflowing hole of the first fixed tube plate is connected with a first graphite heat exchange tube, and the upper side of the overflowing hole of the first fixed tube plate is connected with a first liquid redistribution film former;
a second floating tube plate is arranged inside the joint of the secondary absorption section metal cylinder and the gas-liquid collector, a second graphite heat exchange tube is connected in an overflowing hole of the second floating tube plate, a second circulating water inlet and a second sewage draining outlet are arranged at the lower end of the secondary absorption section metal cylinder, and a second emptying port and a second circulating water outlet are arranged at the upper end of the secondary absorption section metal cylinder; the first circulating water inlet and the second circulating water inlet are respectively connected with a circulating water inlet pipe, and the first circulating water outlet and the second circulating water outlet are respectively connected with a circulating water drain pipe;
the gas-liquid mixer is connected with the second-stage absorption section metal cylinder through a second fixed tube plate, the lower side of an overflowing hole of the second fixed tube plate is connected with a second graphite heat exchange tube, the upper side of the overflowing hole of the second fixed tube plate is connected with a second liquid redistribution film forming device, the lower side of the gas-liquid mixer is provided with a liquid inlet, the liquid inlet is connected with the absorption liquid circulating outlet through a second pipeline, a dilute hydrochloric acid pump is arranged on the second pipeline, a water replenishing pipeline is also connected to the second pipeline between the dilute hydrochloric acid pump and the liquid inlet, and the upper side of the gas-liquid mixer is provided with a gas outlet;
the gas-liquid mixing chamber and the gas-liquid mixer are connected in a blocking manner, the lower side of the gas-liquid mixing chamber is provided with an absorption liquid outlet, and the upper side of the gas-liquid mixing chamber is provided with a second hydrogen chloride gas inlet; the absorption liquid outlet is connected with the alkali liquor preparation tank through a sixth pipeline, the gas outlet and the second hydrogen chloride gas inlet are respectively connected with the vacuum unit through a third pipeline and a fourth pipeline, valves are arranged on the third pipeline and the fourth pipeline, and a fifth pipeline with a valve is arranged between the third pipeline and the fourth pipeline, which are close to one side of the comprehensive absorption tower, of the valve;
the three-stage absorption tower is communicated with the gas-liquid mixing chamber, a filler supporting plate is arranged at the joint of the three-stage absorption tower and the gas-liquid mixing chamber, a filler layer is arranged above the filler supporting plate, a pressure plate is arranged above the filler layer, a sprayer is arranged above the pressure plate, one end of the sprayer is connected with a spraying liquid inlet, the spraying liquid inlet is connected with the alkali liquor preparation tank through a seventh pipeline, an alkali liquor pump is arranged on the seventh pipeline, and a waste alkali liquor discharging pipe with a valve is connected to the seventh pipeline between the alkali liquor pump and the spraying liquid inlet; an upper cover plate is arranged at the top end of the third-stage absorption tower, and a tail gas outlet is arranged on the upper cover plate.
In the antioxidant tail gas recovery processing system, the first graphite heat exchange tube and the second graphite heat exchange tube in the first-stage absorption section metal cylinder and the second-stage absorption section metal cylinder are respectively provided with the first baffle plate and the second baffle plate at the outer sides.
In the antioxidant tail gas recovery processing system, the first liquid redistribution film former and the second liquid redistribution film former are graphite short pipes, and the upper ends of the graphite short pipes are provided with 4V-shaped notches.
In the antioxidant tail gas recovery processing system, the first floating tube plate and the second floating tube plate are connected with the outer tube wall in a sliding sealing manner, and the sliding sealing connection is in a circumferential sealing structure of an O-shaped ring.
In the antioxidant tail gas recovery processing system, the finished product liquid intermediate tank is provided with the first liquid level meter.
In the antioxidant tail gas recovery processing system, the gas-liquid mixing chamber is provided with the second liquid level meter.
In the antioxidant tail gas recovery processing system, the packing layer is a graphite Raschig ring random packing layer.
In the antioxidant tail gas recovery processing system, the overflowing holes of the first fixed tube plate and the second floating tube plate are arranged in a staggered manner.
According to the antioxidant tail gas recovery processing system, the vacuum unit is provided with the circulating water cooling water inlet pipe and the circulating water cooling water outlet pipe, and the circulating water cooling water inlet pipe and the circulating water cooling water outlet pipe are respectively connected with the circulating water inlet pipe and the circulating water drainage pipe.
According to the antioxidant tail gas recovery processing system, the alkali liquor preparation tank is provided with the alkali liquor inlet pipe, the inlet pipe is provided with the stop valve assembly, and the switching of alkali liquor and desalted water can be realized.
In the antioxidant tail gas recovery processing system, the finished hydrochloric acid tank is provided with a finished hydrochloric acid discharge pipe, and the finished hydrochloric acid discharge pipe is provided with a finished hydrochloric acid pump; the top of the finished product hydrochloric acid tank is connected with the alkali liquor preparation tank through an eighth pipeline, and the end part of the eighth pipeline extends into the position below the liquid level in the alkali liquor preparation tank.
The invention has the advantages of
1. Because the reaction speed in the early stage of the reaction is too high and the reaction speed in the later stage is too low during the preparation of the antioxidant, the quality of the antioxidant can be affected, therefore, the invention can reasonably control and adjust the reaction process of the antioxidant by configuring the vacuum unit in the tail gas recovery processing system and installing the vacuum unit at a proper position, controlling the positive pressure value of the reaction system through the pressure regulating valve in the early stage of the reaction, starting the vacuum unit by switching the stop valve to provide and control the negative pressure value in the later stage, and can improve the quality of the antioxidant.
When the antioxidant process system can not recycle the hydrogen chloride, the byproduct hydrochloric acid is the most economical and effective method. The antioxidant tail gas recovery processing system can recycle the byproduct hydrogen chloride gas prepared by the antioxidant 168 to prepare hydrochloric acid, thereby changing waste into valuable.
2. The comprehensive absorption tower is a novel product designed and developed according to the idea of shortening the process flow by strengthening the functional design of equipment. A plurality of operation units such as traditional three-stage absorption, tail gas treatment and the like are integrated in one device to be finished simultaneously; the graphite equipment saves a large amount of accessory equipment and external pipelines, is integrally designed environment-friendly graphite equipment, and has the advantages of compact equipment structure, small occupied space, low investment cost, low operating cost, stable operation, simple operation, convenient installation and maintenance and the like.
3. The invention realizes the process functions of a first-stage falling film absorber, a second-stage falling film absorber, a third-stage water absorption and a third-stage alkali washing, one device independently finishes the absorption of hydrogen chloride, and realizes the functions of tail gas standard reaching and high-altitude emission, and the invention can also realize the instant switching function of the third-stage alkali washing and the third-stage water absorption, and realize the instant switching function of positive pressure and negative pressure of a process system.
4. According to the invention, the floating tube plate structure is arranged in the tower, so that the thermal stress load of the equipment is effectively released, the stress state of the graphite heat exchange tube bundle is improved, the graphite material part only bears the internal pressure load, all external loads of the high tower are uniformly distributed on the metal part, and the problem of low strength of the graphite material is avoided, thereby realizing the design of the high tower made of the graphite material.
5. According to the internal floating tube plate structure, the graphite tube bundle slides in the process of expansion with heat and contraction with cold, the overall dimension of the equipment is not influenced, and an external pipeline and the equipment are not restricted.
6. The graphite tube bundle in the secondary absorption section and the graphite tube bundle in the primary absorption section are in a structural design that the centers of the overflowing holes are distributed on the tube plate in a mutually staggered manner, so that the functions of liquid collection and remixing are effectively realized, a rain-proof cap is not required to be additionally arranged, and the structure of equipment is further simplified.
7. The absorption liquid of the three-stage absorption tower adopts a circulating absorption mode and a countercurrent absorption mode, so that the gas absorption effect is better, and the concentration of the finished hydrochloric acid is easier to control.
The antioxidant tail gas recovery processing system is also suitable for processing waste gases such as ammonia gas, chlorine gas, sulfur dioxide, sulfur trioxide and the like, and is core equipment of a waste gas processing type environment-friendly process system with a wide application range.
Drawings
FIG. 1 is a schematic diagram of the overall structure of the system of the present invention;
FIG. 2 is a schematic structural view of an integrated absorption tower according to the present invention;
FIG. 3 is a schematic structural view of a finished liquid tundish;
FIG. 4 is a schematic structural view of a primary absorption section metal cylinder;
FIG. 5 is a schematic structural view of a metal cylinder of the secondary absorption section;
FIG. 6 is a schematic structural view of a three-stage absorption column;
FIG. 7 is a schematic structural diagram of a second liquid redistribution film former;
fig. 8 is a schematic structural diagram of a conventional exhaust gas treatment system.
Description of reference numerals: 1-circulating outlet of absorption liquid; 2-a first level gauge; 3-finished product liquid intermediate tank; 4-a first hydrogen chloride gas inlet; 5-a first floating tube sheet; 6-a first circulating water inlet; 7-a first baffle plate; 8-a first vent; 9-a first fixed tubesheet; 10-gas-liquid collector; 11-a second circulating water inlet; 12-a second baffle plate; 13-a second vent; 14-a liquid inlet; 15-gas-liquid mixer; 16-an absorption liquid outlet; 17-a gas-liquid mixing chamber; 18-a nip plate; 19-a sprayer; 20-an upper cover plate; 21-gas outlet; 22-spray liquid inlet; 23-a filler layer; 24-a tertiary absorber; 25-a packing support plate; 26-a second level gauge; 27-a second hydrogen chloride gas inlet; 28-gas outlet, 29-second liquid redistribution film former; 30-a second fixed tubesheet; 31-a second circulating water outlet; 32-a secondary absorption section metal cylinder; 33-a second graphite heat exchange tube; 34-a second sewage draining outlet; 35-a second floating tube sheet; 36-a first liquid redistribution film former; 37-a first circulating water outlet; 38-first stage absorption section metal cylinder; 39-a first graphite heat exchange tube; 40-a first drain outlet; 41-upper connecting pipe flange; 42-an absorption liquid inlet; 43-finished product liquid outlet, 44-comprehensive absorption tower, 45-finished product hydrochloric acid tank, 46-vacuum unit, 47-alkali liquor preparation tank, 48-circulating water inlet pipe, 49-circulating water drain pipe, 50-second pipeline, 51-dilute hydrochloric acid pump, 52-water replenishing pipe, 53-fourth pipeline, 54-third pipeline, 55-fifth pipeline, 56-circulating water cooling inlet pipe, 57-circulating water cooling outlet pipe, 58-seventh pipeline, 59-waste alkali liquor discharge pipe, 60-alkali liquor pump, 61-sixth pipeline, 62-alkali liquor feed pipe, 63-first pipeline, 64-finished product hydrochloric acid discharge pipe, 65-concentrated hydrochloric acid pump, 66-finished product hydrochloric acid pump, 67-eighth pipeline, 68-ninth pipeline, and 69-pressure regulating valve.
Detailed Description
The present invention is further illustrated by the following examples, which are not to be construed as limiting the invention.
Examples of the invention
An antioxidant tail gas recovery processing system is shown in figures 1-7, and comprises a comprehensive absorption tower 44, a finished hydrochloric acid tank 45, a vacuum unit 46 and an alkali liquor preparation tank 47; the comprehensive absorption tower 44 comprises a finished product liquid intermediate tank 3, a primary absorption section metal cylinder 38, a gas-liquid collector 10, a secondary absorption section metal cylinder 32, a gas-liquid mixer 15, a gas-liquid mixing chamber 17 and a tertiary absorption tower 24 which are sequentially connected from bottom to top; the finished product liquid intermediate tank 3, the primary absorption section metal cylinder 38, the gas-liquid collector 10, the secondary absorption section metal cylinder 32, the gas-liquid mixer 15, the gas-liquid mixing chamber 17 and the tertiary absorption tower 24 are all made of steel lining high polymer materials, the upper end of the finished product liquid intermediate tank 3 is connected with the primary absorption section metal cylinder 38 through an upper connecting pipe flange 41, and the primary absorption section metal cylinder 38 is connected with the gas-liquid collector 10, the gas-liquid collector 10 is connected with the secondary absorption section metal cylinder 32, the secondary absorption section metal cylinder 32 is connected with the gas-liquid mixer 15, and the gas-liquid mixer 15 is connected with the gas-liquid mixing chamber 17 through flanges; the bottom of the finished product liquid intermediate tank 3 is provided with an absorption liquid circulating outlet 1 and a finished product liquid outlet 43, the finished product liquid outlet 43 is connected with the finished product hydrochloric acid tank 45 through a first pipeline 63, the first pipeline 63 is provided with a concentrated hydrochloric acid pump 65, the middle part of the first pipeline is provided with an absorption liquid inlet 42, the upper part of the first pipeline is provided with a first hydrogen chloride gas inlet 4, the first hydrogen chloride gas inlet 4 is connected with an antioxidant tail gas outlet through a ninth pipeline 68, and the ninth pipeline 68 is provided with a pressure regulating valve 69; a first floating tube plate 5 is arranged inside the joint of the primary absorption section metal cylinder 38 and the finished product liquid intermediate tank 3, a first graphite heat exchange tube 39 is connected in an overflowing hole of the first floating tube plate 5, a first circulating water inlet 6 and a first drain outlet 40 are arranged at the lower end of the primary absorption section metal cylinder 38, and a first vent outlet 8 and a first circulating water outlet 37 are arranged at the upper end of the primary absorption section metal cylinder 38; the gas-liquid collector 10 is connected with the first-stage absorption section metal cylinder 38 through a first fixed tube plate 9, the lower side of an overflowing hole of the first fixed tube plate 9 is connected with a first graphite heat exchange tube 39, and the upper side of the overflowing hole of the first fixed tube plate 9 is connected with a first liquid redistribution film former 36; a second floating tube plate 35 is arranged inside the joint of the second-stage absorption section metal cylinder 32 and the gas-liquid collector 10, a second graphite heat exchange tube 33 is fixedly connected in a flow hole of the second floating tube plate 35, a second circulating water inlet 11 and a second sewage draining outlet 34 are arranged at the lower end of the second-stage absorption section metal cylinder 32, a second vent 13 and a second circulating water outlet 31 are arranged at the upper end of the second floating tube plate, the first circulating water inlet 6 and the second circulating water inlet 11 are respectively connected with a circulating water inlet pipe 48, and the first circulating water outlet 37 and the second circulating water outlet 31 are respectively connected with a circulating water drain pipe 49; the gas-liquid mixer 15 is connected with the second-stage absorption section metal cylinder 32 through a second fixed tube plate 30, the lower side of an overflowing hole of the second fixed tube plate 30 is fixedly connected with a second graphite heat exchange tube 33, the upper side of the overflowing hole of the second fixed tube plate 30 is connected with a second liquid redistribution film former 29, the lower side of the gas-liquid mixer 15 is provided with a liquid inlet 14, the liquid inlet 14 is connected with the absorption liquid circulating outlet 1 through a second pipeline 50, the second pipeline 50 is provided with a dilute hydrochloric acid pump 51, the second pipeline 50 between the dilute hydrochloric acid pump 51 and the liquid inlet 14 is also connected with a water replenishing pipeline 52, the upper side of the gas-liquid mixer 15 is provided with a gas outlet 28, and the upper part of the second liquid redistribution film former 29 is 200mm higher than the liquid inlet 14150; the gas-liquid mixing chamber 17 and the gas-liquid mixer 15 are connected in a blocking way, the lower side of the gas-liquid mixing chamber 17 is provided with an absorption liquid outlet 16, and the upper side is provided with a second hydrogen chloride gas inlet 27; the absorption liquid outlet 16 is connected with the alkali liquor preparation tank 47 through a sixth pipeline 61, the gas outlet 28 and the second hydrogen chloride gas inlet 27 are respectively connected with the vacuum unit 46 through a third pipeline 54 and a fourth pipeline 53, valves are respectively arranged on the third pipeline 54 and the fourth pipeline 53, and a fifth pipeline 55 with a valve is arranged between the third pipeline 54 and the fourth pipeline 53 at one side of the valve close to the comprehensive absorption tower 44; the three-stage absorption tower 24 is in conductive connection with the gas-liquid mixing chamber 17, a filler support plate 25 is arranged at the connection part, a filler layer 23 is arranged above the filler support plate 25, a pressure plate 18 is arranged above the filler layer 23, a sprayer 19 is arranged above the pressure plate 18, one end of the sprayer 19 is connected with a spray liquid inlet 22, the spray liquid inlet 22 is connected with the alkali liquor preparation tank 47 through a seventh pipeline 58, an alkali liquor pump 60 is arranged on the seventh pipeline 58, and a waste alkali liquor discharge pipe 59 with a valve is further connected on the seventh pipeline 58 between the alkali liquor pump 60 and the spray liquid inlet 22; the top end of the third-stage absorption tower 24 is provided with an upper cover plate 20, and the upper cover plate 20 is provided with a tail gas outlet 21.
The working process of the above embodiment is as follows:
1. gas flow path
The hydrogen chloride tail gas continuously enters the upper space of the finished product liquid intermediate tank 3 through the first hydrogen chloride gas inlet 4, the discharge speed of a byproduct hydrogen chloride gas is controlled through the pressure regulating valve 69 in the early stage of reaction, the positive pressure value of the antioxidant reaction system is further controlled, the hydrogen chloride tail gas further flows upwards into the first graphite heat exchange tube 39 of the first-stage absorption section graphite heat exchange tube bundle, countercurrent contact mass transfer is carried out on an absorption liquid film flowing downwards along the inner wall with the first graphite heat exchange tube 39, the hydrogen chloride gas is absorbed and releases absorption heat, and the absorption heat is taken away by shell pass cooling water on the service side of the first-stage absorption section in a wall type heat exchange mode, so that the absorption is carried out towards a favorable.
The unabsorbed hydrogen chloride gas continuously enters the gas-liquid collector 10 upwards, is mixed and redistributed, flows upwards into the second graphite heat exchange tube 33 of the second-stage absorption section graphite heat exchange tube bundle, and is subjected to countercurrent contact mass transfer with an absorption liquid film flowing downwards along the inner wall of the second graphite heat exchange tube 33, the hydrogen chloride gas is absorbed and releases absorption heat, and the absorption heat is taken away by shell pass cooling water on the service side of the second-stage absorption section in a dividing wall type heat exchange mode, so that the absorption is carried out towards a favorable direction.
The residual unabsorbed trace hydrogen chloride gas and the impurity tail gas continuously enter the gas-liquid mixer 15 upwards, are converged and mixed, then flow out of the gas-liquid mixer 15 through the gas outlet 28, and then sequentially enter the gas-liquid mixing chamber 17 at the lower part of the third-stage absorption tower 24 through the third pipeline 54, the fifth pipeline 55, the fourth pipeline 53 and the second hydrogen chloride gas inlet 27; further upwards passes through a graphite Raschig ring bulk stack filler layer 23, countercurrent contact, mass transfer and heat transfer are carried out on the surface of the filler and absorption liquid, residual micro hydrogen chloride gas in tail gas is absorbed, simultaneously released heat energy is also taken away by the absorption liquid, and impurity tail gas which is difficult to dissolve is discharged after reaching standards at high altitude through a gas outlet 21 arranged on an upper cover plate 20; the process tasks of absorbing hydrogen chloride gas in the tail gas and treating the tail gas are completed; in the process, when the antioxidant reaction is in the initial stage, the tail gas is discharged by means of internal positive pressure and flows through the path, at the moment, the vacuum unit 46 does not need to work, namely, the valves on the third pipeline 54 and the fourth pipeline 53 are closed, the valve on the fifth pipeline 55 is opened, and the tail gas naturally circulates; when the reaction is carried out to the later stage, the tail gas generated in the reaction device is insufficient, hydrogen chloride gas is very little, but the hydrogen chloride gas needs to be discharged in time, at the moment, the valves on the vacuum unit 46, the third pipeline 54 and the fourth pipeline 53 are opened, the valve on the fifth pipeline 55 is closed, and the tail gas is timely pumped out and treated by using the negative pressure generated by the vacuum unit 46.
2. Path of flow of absorption liquid
Deionized water enters the gas-liquid mixer 15 through the water supplementing pipeline 52, gradually becomes stable after the liquid level rises by 150-mm, reaches the upper end of the liquid film distributor 29, enters second liquid, is divided into the inner wall of the film distributor 29 to form an acidic absorption liquid film, further enters the second graphite heat exchange tube 33 of the graphite heat exchange tube bundle of the secondary absorption section in a downward mode, and is in countercurrent contact mass transfer with continuous upward tail gas which is not absorbed by the primary absorption section in the second graphite heat exchange tube 33, after the acidic absorption liquid film absorbs hydrogen chloride gas, the concentration of hydrochloric acid is gradually increased, and the hydrochloric acid gradually becomes dilute hydrochloric acid and flows downward into the gas-liquid collector 10.
In the process section, the hydrogen chloride gas is absorbed and releases absorption heat, the temperature of the dilute hydrochloric acid is raised, meanwhile, the shell-side cooling water on the service side of the secondary absorption section enters the secondary absorption section metal cylinder 32 through the second circulating water inlet 11, the wall-type heat exchange is carried out between the inner wall and the outer wall of the second graphite heat exchange tube 33 of the secondary absorption section graphite heat exchange tube bundle, the absorption heat is taken away in time, the temperature of the dilute hydrochloric acid is controlled not to rise continuously, the absorption process is carried out towards the favorable direction, and the shell-side cooling water on the service side completing the heat exchange process task flows out of the secondary absorption section metal cylinder 32 through the second circulating water outlet 31.
After the dilute hydrochloric acid flows into the gas-liquid collector 10, the liquid collecting and remixing functions are realized.
The liquid level gradually tends to be stable after rising, the liquid level reaches the upper end of the first liquid redistribution film former 36, the liquid enters the inner wall of the first liquid redistribution film former 36 through the upper end to form a downward dilute hydrochloric acid liquid film, the liquid further enters the first graphite heat exchange tube 39 of the graphite heat exchange tube bundle of the primary absorption section in a descending manner, the liquid and the upward hydrogen chloride gas to be treated in the first graphite heat exchange tube 39 are subjected to countercurrent contact mass transfer, after the dilute hydrochloric acid liquid film absorbs the hydrogen chloride gas, the concentration of hydrochloric acid is gradually increased, the hydrochloric acid is gradually changed into slightly concentrated hydrochloric acid, and the slightly concentrated hydrochloric acid flows downwards into the finished product liquid intermediate tank 3, so that the.
In the process section, the hydrogen chloride gas is absorbed and releases absorption heat, the temperature of the concentrated hydrochloric acid rises, meanwhile, shell pass cooling water on the service side of the primary absorption section enters the primary absorption section metal cylinder 38 through the first circulating water inlet 6, the inside and outside walls of the first graphite heat exchange tube 39 of the graphite heat exchange tube bundle of the primary absorption section are subjected to wall-dividing type heat exchange, the absorption heat is taken away in time, the temperature of the concentrated hydrochloric acid is controlled not to rise continuously, the absorption process is carried out towards the favorable direction, and the shell pass cooling water on the service side completing the heat exchange process task flows out of the secondary absorption section metal cylinder 38 through the first circulating water outlet 37.
The hydrochloric acid solution flowing into the finished product liquid intermediate tank 3 does not reach the standard of concentrated hydrochloric acid initially, then the hydrochloric acid solution in the finished product liquid intermediate tank 3 is pumped into the gas-liquid mixer 15 through the dilute hydrochloric acid pump 51 to repeatedly absorb hydrogen chloride, and after the hydrochloric acid solution reaches the standard, the hydrochloric acid solution is conveyed into the finished product hydrochloric acid tank 45 through the finished product hydrochloric acid pump 66 to be stored; meanwhile, when the tail gas enters the tertiary absorption tower 24, the alkali liquor in the alkali liquor preparation tank 47 is sent to the sprayer 19 through the alkali liquor pump 60, part of the tail gas is sprayed, the tail gas reaches the final emission standard, the alkali liquor returns to the alkali liquor preparation tank 47 through the sixth pipeline 61, and when the alkali liquor cannot be reused, the alkali liquor is discharged from the waste alkali liquor discharge pipe 59, but only when the tail gas enters the tertiary absorption tower 24, the tail gas also contains more hydrogen chloride or other harmful acid gases, and the effect of tail gas treatment can be improved by using the alkali liquor; when hydrogen chloride or other harmful gases entering the tertiary absorption tower 24 can be absorbed by water, the alkali liquor in the alkali liquor preparation tank 47 can be replaced by deionized water, and water washing can be performed according to the alkali washing process.
Preferably, the first baffle 7 and the second baffle 12 are respectively disposed at the outer sides of the first graphite heat exchange tube 39 and the second graphite heat exchange tube 33 in the first-stage absorption section metal cylinder 38 and the second-stage absorption section metal cylinder 32, and the flow direction of the cooling water can be controlled and the heat exchange efficiency can be improved under the action of the first baffle 7 and the second baffle 12.
Preferably, the first liquid redistribution film forming device 36 and the second liquid redistribution film forming device 29 are graphite short tubes, and the upper ends of the graphite short tubes are provided with 4V-shaped notches. The absorption liquid tangentially and vertically enters the inner wall of the liquid redistribution film-forming device through a liquid flow channel with 4V-shaped notches formed at the upper end to form an acidic absorption liquid film with downward rotational flow.
Preferably, the first floating tube plate 5 and the second floating tube plate 35 are connected with the outer tube wall in a sliding and sealing manner, and the structure of the sliding and sealing connection is an O-ring circumferential sealing structure.
Preferably, the product liquid intermediate tank 3 is provided with a first liquid level meter 2. The flow and the liquid level of the acidic absorption liquid in the finished product liquid intermediate tank 3 are observed and controlled by the first liquid level meter 2.
Preferably, the gas-liquid mixing chamber 17 is provided with a second liquid level gauge 26. The flow rate and the liquid level of the acidic absorbent in the gas-liquid mixing chamber 17 are observed and controlled by the second level meter 26.
Preferably, the overflowing holes of the first fixed tube plate 9 and the second floating tube plate 35 are arranged in a staggered mode. Because the overflowing holes of the first fixed tube plate 9 and the second floating tube plate 35 are arranged in a staggered mode, 17% of dilute hydrochloric acid can directly fall to the bottom of the gas-liquid collector 10 without an additional rain-proof cap after flowing into the gas-liquid collector 10, and the function of collecting and remixing liquid is achieved.
Preferably, the vacuum unit 46 is provided with a circulating water cooling water inlet pipe 56 and a circulating water cooling water outlet pipe 57, the circulating water cooling water inlet pipe 56 and the circulating water cooling water outlet pipe 57 are respectively connected with the circulating water inlet pipe 48 and the circulating water drain pipe 49, and when tail gas passes through the vacuum unit 46, the circulating water cooling water inlet pipe 56 and the circulating water cooling water outlet pipe 57 take away heat on the vacuum unit 46 in time.
Preferably, the lye preparing tank 47 is provided with a lye feeding pipe 62.
Preferably, a finished hydrochloric acid discharge pipe 64 is arranged on the finished hydrochloric acid tank 45, and a finished hydrochloric acid pump 66 is arranged on the finished hydrochloric acid discharge pipe 64; the top of the finished hydrochloric acid tank 45 is connected with the alkali liquor preparation tank 47 through an eighth pipeline 67, the end part of the eighth pipeline 67 extends into the position below the liquid level in the alkali liquor preparation tank 47, a small amount of hydrogen chloride gas is generated in the process of storing concentrated hydrochloric acid, and air pollution can be caused if the finished hydrochloric acid tank 45 is directly emptied, so that the hydrogen chloride gas is introduced into the position below the liquid level in the alkali liquor preparation tank 47 through the eighth pipeline 67 to complete water sealing and avoid overflowing.
The structural integrity of the system is stronger by comparing fig. 1 and fig. 8, and the tail gas recycling system with model number DN400 × 9500 designed and developed by the present application is compared with the existing system in terms of performance and price in 13 aspects, which is detailed in table one.
Table one: performance comparison table of system of the invention and the existing system
Note: by combining the performance comparison conditions of the 13 factors, the system has superior performance and low cost, and has more comprehensive advantages compared with similar functional products in the market.
The above description is only for the purpose of illustrating the present invention and the appended claims, and the scope of the present invention is not limited thereto, and any person skilled in the art can substitute or change the technical solution and the inventive concept of the present invention within the technical scope of the present invention.
Claims (10)
1. The utility model provides an anti-oxidant tail gas recovery processing system which characterized in that: comprises a comprehensive absorption tower (44), a finished hydrochloric acid tank (45), a vacuum unit (46) and an alkali liquor preparation tank (47);
the comprehensive absorption tower (44) comprises a finished product liquid intermediate tank (3), a primary absorption section metal cylinder (38), a gas-liquid collector (10), a secondary absorption section metal cylinder (32), a gas-liquid mixer (15), a gas-liquid mixing chamber (17) and a tertiary absorption tower (24) which are sequentially connected from bottom to top;
an absorption liquid circulating outlet (1) and a finished product liquid outlet (43) are arranged at the bottom of the finished product liquid intermediate tank (3), the finished product liquid outlet (43) is connected with the finished product hydrochloric acid tank (45) through a first pipeline (63), a concentrated hydrochloric acid pump (65) is arranged on the first pipeline (63), an absorption liquid inlet (42) is arranged in the middle of the first pipeline, a first hydrogen chloride gas inlet (4) is arranged at the upper part of the first pipeline, the first hydrogen chloride gas inlet (4) is connected with an antioxidant tail gas outlet through a ninth pipeline (68), and a pressure regulating valve (69) is arranged on the ninth pipeline (68);
a first floating tube plate (5) is arranged inside the joint of the primary absorption section metal cylinder (38) and the finished product liquid intermediate tank (3), a first graphite heat exchange tube (39) is connected in an overflowing hole of the first floating tube plate (5), a first circulating water inlet (6) and a first drain outlet (40) are arranged at the lower end of the primary absorption section metal cylinder (38), and a first drain outlet (8) and a first circulating water outlet (37) are arranged at the upper end of the primary absorption section metal cylinder;
the gas-liquid collector (10) is connected with the first-stage absorption section metal cylinder (38) through a first fixed tube plate (9), the lower side of an overflowing hole of the first fixed tube plate (9) is connected with a first graphite heat exchange tube (39), and the upper side of the overflowing hole of the first fixed tube plate (9) is connected with a first liquid redistribution film former (36);
a second floating tube plate (35) is arranged inside the joint of the secondary absorption section metal cylinder (32) and the gas-liquid collector (10), a second graphite heat exchange tube (33) is connected in an overflowing hole of the second floating tube plate (35), a second circulating water inlet (11) and a second sewage outlet (34) are arranged at the lower end of the secondary absorption section metal cylinder (32), and a second vent hole (13) and a second circulating water outlet (31) are arranged at the upper end of the secondary absorption section metal cylinder; the first circulating water inlet (6) and the second circulating water inlet (11) are respectively connected with a circulating water inlet pipe (48), and the first circulating water outlet (37) and the second circulating water outlet (31) are respectively connected with a circulating water drain pipe (49);
the gas-liquid mixer (15) is connected with the second-stage absorption section metal cylinder (32) through a second fixed tube plate (30), the lower side of an overflowing hole of the second fixed tube plate (30) is connected with a second graphite heat exchange tube (33), the upper side of the overflowing hole of the second fixed tube plate (30) is connected with a second liquid redistribution film-forming device (29), the lower side of the gas-liquid mixer (15) is provided with a liquid inlet (14), the liquid inlet (14) is connected with the absorption liquid circulation outlet (1) through a second pipeline (50), the second pipeline (50) is provided with a dilute hydrochloric acid pump (51), the second pipeline (50) between the dilute hydrochloric acid pump (51) and the liquid inlet (14) is also connected with a water replenishing pipeline (52), and the upper side of the gas-liquid mixer (15) is provided with a gas outlet (28);
the gas-liquid mixing chamber (17) and the gas-liquid mixer (15) are connected in a blocking way, the lower side of the gas-liquid mixing chamber (17) is provided with an absorption liquid outlet (16), and the upper side is provided with a second hydrogen chloride gas inlet (27); an absorption liquid outlet (16) is connected with the alkali liquor preparation tank (47) through a sixth pipeline (61), a gas outlet (28) and a second hydrogen chloride gas inlet (27) are respectively connected with the vacuum unit (46) through a third pipeline (54) and a fourth pipeline (53), valves are respectively arranged on the third pipeline (54) and the fourth pipeline (53), and a fifth pipeline (55) with a valve is arranged between the third pipeline (54) and the fourth pipeline (53) on one side of the valve close to the comprehensive absorption tower (44);
the three-stage absorption tower (24) is in conduction connection with the gas-liquid mixing chamber (17), a filler supporting plate (25) is arranged at the joint, a filler layer (23) is arranged above the filler supporting plate (25), a pressure plate (18) is arranged above the filler layer (23), a sprayer (19) is arranged above the pressure plate (18), one end of the sprayer (19) is connected with a spraying liquid inlet (22), the spraying liquid inlet (22) is connected with the alkali liquor preparation tank (47) through a seventh pipeline (58), an alkali liquor pump (60) is arranged on the seventh pipeline (58), and a waste alkali liquor discharging pipe (59) with a valve is further connected to the seventh pipeline (58) between the alkali liquor pump (60) and the spraying liquid inlet (22); an upper cover plate (20) is arranged at the top end of the third-stage absorption tower (24), and a tail gas outlet (21) is arranged on the upper cover plate (20).
2. The antioxidant tail gas recovery processing system of claim 1, characterized in that: and a first baffle plate (7) and a second baffle plate (12) are respectively arranged on the outer sides of the first graphite heat exchange tube (39) and the second graphite heat exchange tube (33) in the first-stage absorption section metal cylinder (38) and the second-stage absorption section metal cylinder (32).
3. The antioxidant tail gas recovery processing system of claim 1, characterized in that: the first liquid redistribution film forming device (36) and the second liquid redistribution film forming device (29) are short graphite pipes, and the upper ends of the short graphite pipes are provided with 4V-shaped notches.
4. The antioxidant tail gas recovery processing system of claim 1, characterized in that: the first floating tube plate (5) and the second floating tube plate (35) are connected with the outer tube wall in a sliding sealing mode, and the sliding sealing connection mode is an O-shaped ring circumferential sealing structure.
5. The antioxidant tail gas recovery processing system of claim 1, characterized in that: a first liquid level meter (2) is arranged on the finished product liquid intermediate tank (3); and a second liquid level meter (26) is arranged on the gas-liquid mixing chamber (17).
6. The antioxidant tail gas recovery processing system of claim 1, characterized in that: the filler layer (23) is a graphite Raschig ring random stack filler layer.
7. The antioxidant tail gas recovery processing system of claim 1, characterized in that: and the overflowing holes of the first fixed tube plate (9) and the second floating tube plate (35) are arranged in a staggered mode.
8. The antioxidant tail gas recovery processing system of claim 1, characterized in that: and the vacuum unit (46) is provided with a circulating water cooling water inlet pipe (56) and a circulating water cooling water outlet pipe (57), and the circulating water cooling water inlet pipe (56) and the circulating water cooling water outlet pipe (57) are respectively connected with the circulating water inlet pipe (48) and the circulating water drain pipe (49).
9. The antioxidant tail gas recovery processing system of claim 1, characterized in that: an alkali liquor feeding pipe (62) is arranged on the alkali liquor preparation tank (47).
10. The antioxidant tail gas recovery processing system of claim 1, characterized in that: a finished hydrochloric acid discharge pipe (64) is arranged on the finished hydrochloric acid tank (45), and a finished hydrochloric acid pump (66) is arranged on the finished hydrochloric acid discharge pipe (64); the top of the finished product hydrochloric acid tank (45) is connected with the alkali liquor preparation tank (47) through an eighth pipeline (67), and the end part of the eighth pipeline (67) extends into the liquid level in the alkali liquor preparation tank (47).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010394023.0A CN111495123A (en) | 2020-05-11 | 2020-05-11 | Antioxidant tail gas recovery processing system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010394023.0A CN111495123A (en) | 2020-05-11 | 2020-05-11 | Antioxidant tail gas recovery processing system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111495123A true CN111495123A (en) | 2020-08-07 |
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ID=71875486
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010394023.0A Pending CN111495123A (en) | 2020-05-11 | 2020-05-11 | Antioxidant tail gas recovery processing system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111495123A (en) |
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2020
- 2020-05-11 CN CN202010394023.0A patent/CN111495123A/en active Pending
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