CN212327825U - Organic waste gas treatment system for producing hydrogen peroxide by anthraquinone process - Google Patents
Organic waste gas treatment system for producing hydrogen peroxide by anthraquinone process Download PDFInfo
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Abstract
The utility model belongs to the technical field of chemical production, in particular to an organic waste gas treatment system for producing hydrogen peroxide by an anthraquinone method, which comprises a cooling condensation separation system and an active carbon adsorption system; the cooling condensation separation system comprises a primary cooler, a primary separator, a secondary cooler and a secondary separator; the active carbon adsorption system comprises at least three active carbon adsorption tanks, and a cooler, a separation tank, a metering tank, a fan, a vortex air pump, a control valve and a DCS control system which are matched with the active carbon adsorption tanks; the utility model reduces the temperature of the emptied organic waste gas by the fractional condensation separation method, so that the content of heavy aromatics is reduced, and then VOCs of the organic waste gas are further reduced by two-stage or multi-stage activated carbon adsorption, so as to realize the standard discharge of the VOCs; furthermore, through the utility model provides an organic waste gas treatment system can also retrieve a large amount of arene, has reduced manufacturing cost.
Description
Technical Field
The utility model belongs to the technical field of chemical production, concretely relates to organic waste gas treatment system of anthraquinone process production hydrogen peroxide solution.
Background
With the progress of science and technology, the quality of life of people is improved, and the requirement on environmental protection is higher and higher. The environmental pollution is mainly caused by three wastes formed in the industrial production process and the life of people; particularly, petrochemical enterprises can emit a large amount of waste gas in the production process, wherein the emission of volatile organic waste gas is regarded as the second main type of atmospheric pollutants, and is second only to atmospheric particulate matters. With the emphasis of the country on environmental protection and the increase of the environmental protection treatment, the organic waste gas generated in the production process must be treated by enterprises and discharged after reaching the standard, but the organic waste gas is generally directly discharged into the atmosphere after being simply treated by the traditional chemical enterprises in the production process, so that the emission standard that VOCs is less than or equal to 120mg/m3 cannot be reached, and serious atmospheric pollution is caused.
In the prior art, the anthraquinone method is the most important method for producing hydrogen peroxide, and the process comprises the steps of preparing a working solution from alkyl anthraquinone and an organic solvent, introducing hydrogen for hydrogenation under the conditions that the pressure is 0.30MPa, the temperature is 55-65 ℃ and a catalyst exists, performing countercurrent oxidation with air (or oxygen) at 40-44 ℃, and preparing a hydrogen peroxide aqueous solution product with the mass fraction of 20-30% through extraction, regeneration, refining and concentration. In the process of producing hydrogen peroxide by the anthraquinone method, if organic waste gas cannot be reasonably treated, the atmosphere can be polluted.
For example, chinese patent publication No. CN108057309A essentially discloses a recycling apparatus for organic waste gas, which is characterized in that: the organic waste gas is pretreated firstly and is subjected to two-stage treatment by an activated carbon fiber box, so that the recovery amount of organic solvents in the organic waste gas is improved, but the up-to-standard discharge of VOCs in the organic waste gas is not realized; meanwhile, the device only has four processes of adsorption, desorption, cooling and drying, and particularly can blow out part of organic solvent steam remained in the activated carbon after steam desorption from the air when a fan is dried and exhausted, so that emission detection data is influenced, and meanwhile, the field has smell.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the defects in the prior art and provide an organic waste gas treatment system for producing hydrogen peroxide by an anthraquinone method.
In order to achieve the above purpose, the utility model adopts the following technical scheme to realize:
an organic waste gas treatment system for producing hydrogen peroxide by an anthraquinone process comprises a cooling condensation separation system and an active carbon adsorption system;
the cooling condensation separation system comprises a primary cooler, a primary separator, a secondary cooler and a secondary separator; cooling the organic waste gas to be treated by a first-stage cooler, separating by a first-stage separator, cooling by a second-stage cooler, and separating by a second-stage separator;
the active carbon adsorption system comprises at least three active carbon adsorption tanks, and a cooler, a separation tank, a metering tank, a fan, a vortex air pump, a control valve and a DCS control system which are matched with the active carbon adsorption tanks;
every two activated carbon adsorption tanks are connected through a valve and a pipeline to form a primary and secondary adsorption process, organic solvent in the organic waste gas is discharged after being adsorbed by the activated carbon adsorption tanks, the activated carbon adsorption tanks adsorbing the organic solvent are subjected to steam desorption, condenser condensation and separation tank separation to obtain the organic solvent for recovery, and the desorbed water is led to a sewage station for treatment.
In a further technical solution, the organic waste gas treatment system further comprises: the storage tank is in an unorganized discharge and recovery system,
the device comprises a pipeline, a cooler, a separation tank and a vortex air pump; the unorganized emptying gas of each storage tank passes through a pipeline, is cooled, condensed and separated by a cooler and a separating tank, and is pumped into the activated carbon adsorption system by a vortex gas pump for treatment.
In a further technical scheme, the activated carbon adsorption system comprises three activated carbon adsorption tanks, namely a first activated carbon adsorption tank, a second activated carbon adsorption tank and a third activated carbon adsorption tank;
a tail gas main valve is arranged on an input pipe of the activated carbon adsorption system, and the other end of the tail gas main valve is connected to the air inlet end of the bottom of the first activated carbon adsorption tank through a first air release valve, connected to the air inlet end of the bottom of the second activated carbon adsorption tank through a second air release valve and connected to the air inlet end of the bottom of the third activated carbon adsorption tank through a third air release valve;
the outlet duct of first active carbon adsorption jar divide into three routes: one path is discharged through a first discharge valve and then is communicated to the air inlet end at the bottom of the first activated carbon adsorption tank through a first inlet valve, is communicated to the air inlet end at the bottom of the second activated carbon adsorption tank through a second inlet valve, and is communicated to the air inlet end at the bottom of the third activated carbon adsorption tank through a third inlet valve; one path is discharged through a first air outlet valve; one path of the air is connected to a cooler through a first drying valve, and is connected to an input pipe of the activated carbon adsorption system through a vacuum valve and a vortex air pump;
the outlet duct of second active carbon adsorption jar divide into three routes: one path is discharged through a second joint outlet valve and then is communicated to the air inlet end at the bottom of the first activated carbon adsorption tank through a first joint inlet valve, is communicated to the air inlet end at the bottom of the second activated carbon adsorption tank through the second joint inlet valve, and is communicated to the air inlet end at the bottom of the third activated carbon adsorption tank through a third joint inlet valve; one path is discharged through a second air outlet valve; one path of the air is connected to a cooler through a second drying valve, and is connected to an input pipe of the activated carbon adsorption system through a vacuum valve and a vortex air pump;
the outlet duct of the third activated carbon adsorption tank is divided into three paths: one path is discharged through a third discharge valve and then is communicated to the air inlet end at the bottom of the first activated carbon adsorption tank through a first joint inlet valve, is communicated to the air inlet end at the bottom of the second activated carbon adsorption tank through a second joint inlet valve, and is communicated to the air inlet end at the bottom of the third activated carbon adsorption tank through a third joint inlet valve; one path is discharged through a third air outlet valve; one path of the air is connected to a cooler through a third drying valve, and is connected to an input pipe of the activated carbon adsorption system through a vacuum valve and a vortex air pump;
the air outlet end of the cooler is divided into two paths: one path is discharged through a condensing valve, and is communicated to the air inlet end at the bottom of the first activated carbon adsorption tank through a first steam outlet valve, communicated to the air inlet end at the bottom of the second activated carbon adsorption tank through a second steam outlet valve, and communicated to the air inlet end at the bottom of the third activated carbon adsorption tank through a third steam outlet valve;
one path is communicated to the air inlet end of the fan through an external drying valve; the air outlet end of the fan is discharged through an inner drying valve; the first steam outlet valve is communicated with the air inlet end at the bottom of the first activated carbon adsorption tank, the second steam outlet valve is communicated with the air inlet end at the bottom of the second activated carbon adsorption tank, and the third steam outlet valve is communicated with the air inlet end at the bottom of the third activated carbon adsorption tank;
the liquid outlet end of the cooler is connected to a separation tank through a liquid discharge valve, and the separation tank is connected to a metering tank through a pipeline;
the separation groove and the metering groove are respectively communicated to the air inlet end of the vortex air pump through an exhaust valve and a vacuum valve;
the first activated carbon adsorption tank is connected with a steam pipeline with a first steam inlet valve, the second activated carbon adsorption tank is connected with a steam pipeline with a second steam inlet valve, and the third activated carbon adsorption tank is connected with a steam pipeline with a third steam inlet valve;
and the input pipe of the activated carbon adsorption system is also connected with a pipeline with an emptying valve.
Compared with the prior art, the utility model discloses following technological effect has:
the utility model provides an organic waste gas treatment system of anthraquinone process production hydrogen peroxide solution, through fractional condensation separation's method, to the temperature reduction of emptying organic waste gas, can make the content of heavy aromatics reduce, then, rethread second grade or multistage active carbon adsorption further reduce organic waste gas's VOCs to realize VOCs's discharge to reach standard, in addition, through the utility model provides an organic waste gas treatment system can also retrieve a large amount of aromatics, has reduced manufacturing cost.
Drawings
FIG. 1 is a schematic view of an organic waste gas treatment system for producing hydrogen peroxide by an anthraquinone process;
fig. 2 is a schematic view of an activated carbon adsorption system provided by the present invention;
FIG. 3 is a flow chart of the adsorption and steam desorption condensation process of the activated carbon adsorption tank of the present invention;
FIG. 4 is a flow chart of the process of vacuum pumping and fan drying of the activated carbon adsorption tank of the present invention;
the reference numbers in the figures illustrate: 1-a first activated carbon adsorption tank, 2-a second activated carbon adsorption tank, 3-a third activated carbon adsorption tank, 4-a cooler, 5-a blower, 6-a vortex air pump, 7-a separation tank, 8-a metering tank, 11-a first air release valve, 21-a second air release valve, 31-a third air release valve, 12-a first joint inlet valve, 22-a second joint inlet valve, 32-a third joint inlet valve, 13-a first steam outlet valve, 23-a second steam outlet valve, 33-a third steam outlet valve, 14-a first joint outlet valve, 24-a second joint outlet valve, 34-a third joint outlet valve, 15-a first outlet valve, 25-a second outlet valve, 35-a third outlet valve, 16-a first drying valve, 26-a second drying valve, 36-a third drying valve, 17-a first steam inlet valve, 27-a second steam inlet valve, 37-a third steam inlet valve, 41-a tail gas main valve, 42-an emptying valve, 43-a condensing valve, 44-an internal drying valve, 45-an external drying valve, 46-a liquid discharge valve, 47-a vacuum valve and 48-an exhaust valve.
Detailed Description
In order to make the technical means, creation characteristics, achievement purpose and efficacy of the utility model easy to understand and understand, the utility model is further clarified by combining the specific drawings.
It should be noted that, in the present invention, when an element is referred to as being "fixed" to another element, it may be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. The terms "vertical," "horizontal," "left," "right," and the like as used herein are for illustrative purposes only and do not denote a unique embodiment.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed items.
As shown in figure 1, the utility model provides an organic waste gas treatment system for producing hydrogen peroxide by an anthraquinone method, which comprises a cooling condensation separation system and an active carbon adsorption system;
the cooling condensation separation system comprises a primary cooler, a primary separator, a secondary cooler and a secondary separator; cooling the organic waste gas to be treated by a first-stage cooler, separating by a first-stage separator, cooling by a second-stage cooler, and separating by a second-stage separator;
the active carbon adsorption system comprises at least three active carbon adsorption tanks, and a cooler, a separation tank, a metering tank, a fan, a vortex air pump, a control valve and a DCS control system which are matched with the active carbon adsorption tanks;
every two activated carbon adsorption tanks are connected through a valve and a pipeline to form a primary and secondary adsorption process, organic solvent in the organic waste gas is discharged after being adsorbed by the activated carbon adsorption tanks, the activated carbon adsorption tanks adsorbing the organic solvent are subjected to steam desorption, condenser condensation and separation tank separation to obtain the organic solvent for recovery, and the desorbed water is led to a sewage station for treatment.
Furthermore, the organic waste gas treatment system also comprises a storage tank unorganized discharge recovery system, wherein the storage tank unorganized discharge recovery system comprises a pipeline, a cooler, a separation tank and a vortex air pump; the unorganized emptying gas of each storage tank passes through a pipeline, is cooled, condensed and separated by a cooler and a separating tank, and is pumped into the activated carbon adsorption system by a vortex gas pump for treatment.
Through the above organic waste gas treatment system provided by the utility model, in the specific treatment process, the organic waste gas controlled by the pressure of the emptying system, namely the oxidized tail gas in figure 1 passes through the primary cooler and the primary separator, and is cooled to 28-32 ℃ by circulating water; then continuously passing through a secondary cooler and a secondary separator, and cooling to 3-7 ℃; then introducing the mixture into an activated carbon adsorption system for further treatment; and recycling the separated organic solvent.
Specifically, for example, the oxidation tail gas at about 50 ℃ in the system for producing hydrogen peroxide by the anthraquinone method passes through a primary cooler by system pressure, is cooled to about 30 ℃ by circulating water, and part of organic solvent in the oxidation tail gas is cooled, condensed and separated by a primary separator; then, the oxidized tail gas at about 30 ℃ continuously passes through a secondary cooler, the temperature is reduced to about 5 ℃ by low-temperature water or an expansion refrigerating unit, and then the organic solvent in the oxidized tail gas is further cooled, condensed and separated out through a secondary separator; introducing the treated oxidation tail gas into an active carbon adsorption system for further treatment; through the treatment system, the organic solvent of the oxidation tail gas is fully separated, and the requirement of standard emission is met; and the separated organic solvent can be recycled.
In the utility model, in order to improve the separation effect on the organic solvent, the primary cooler is internally provided with internals such as a diaphragm separator, a stainless steel wire mesh demister and the like; and the secondary cooler is internally provided with internals such as a stainless steel wire mesh demister, a high-efficiency separation filter element and the like.
The technical scheme provided by the utility model, to the characteristics that organic waste gas is heavy aromatics (the principal ingredients is C9 trimethylbenzene) in anthraquinone method production hydrogen peroxide, according to the relation curve of aromatic content and temperature, through fractional condensation separation's method, reduce the organic waste gas of unloading about 5 ℃ from 50 ℃, can make the content of heavy aromatics reduce to 12% (content is about 1700 mg/m)3) (ii) a Then the organic waste gas is reduced to 120mg/m by a two-stage or multi-stage active carbon adsorption system3Realizing the standard discharge of VOCs; in addition, the treatment system of the utility model can recover a large amount of aromatic hydrocarbon, thereby reducing the production cost; on the other hand, the utility model provides a method can realize automaticly, has easy operation, and the running cost is low, and purification efficiency is high, safe advantage economic again promptly.
The utility model provides an among the organic waste gas treatment system, with each storage tank unorganized atmospheric air pass through the pipeline in the anthraquinone method production hydrogen peroxide system, cool down the condensation separation back through cooler and knockout drum earlier, rethread vortex gas pump send extremely active carbon adsorption system in handle. That is, the utility model provides a treatment system still can be compatible to the processing of each storage tank unorganized unloading gas, has realized having organized and the synchronous processing of each storage tank unorganized unloading gas.
Fig. 2 is a schematic view of an activated carbon adsorption system provided by the present invention; the active carbon adsorption system comprises three active carbon adsorption tanks, and a cooler 4, a separation tank 7, a metering tank 8, a fan 5, a vortex air pump 6, a control valve and a DCS control system which are matched with the active carbon adsorption tanks; the three activated carbon adsorption tanks are respectively a first activated carbon adsorption tank 1, a second activated carbon adsorption tank 2 and a third activated carbon adsorption tank 3;
a tail gas main valve 41 is arranged on an input pipe of the activated carbon adsorption system, the other end of the tail gas main valve 41 is connected to the air inlet end at the bottom of the first activated carbon adsorption tank 1 through a first air release valve 11, is connected to the air inlet end at the bottom of the second activated carbon adsorption tank 2 through a second air release valve 21, and is connected to the air inlet end at the bottom of the third activated carbon adsorption tank 3 through a third air release valve 31;
the outlet duct of the first activated carbon adsorption tank 1 is divided into three paths: one path is discharged through a first discharge valve 14 and then communicated to the air inlet end at the bottom of the first activated carbon adsorption tank 1 through a first inlet valve 12, communicated to the air inlet end at the bottom of the second activated carbon adsorption tank 2 through a second inlet valve 22, and communicated to the air inlet end at the bottom of the third activated carbon adsorption tank 3 through a third inlet valve 32; one path is discharged through a first air outlet valve 15; one path is connected to the cooler 4 through the first drying valve 16, and is connected to the input pipe of the activated carbon adsorption system through the vacuum valve 47 and the vortex air pump 6;
the outlet duct of the second activated carbon adsorption tank 2 is divided into three paths: one path is discharged through a second coupling outlet valve 24 and then communicated to the air inlet end at the bottom of the first activated carbon adsorption tank 1 through a first coupling inlet valve 12, communicated to the air inlet end at the bottom of the second activated carbon adsorption tank 2 through a second coupling inlet valve 22 and communicated to the air inlet end at the bottom of the third activated carbon adsorption tank 3 through a third coupling inlet valve 32; one path is discharged through a second air outlet valve 25; one path is connected to the cooler 4 through the second drying valve 26, and is connected to the input pipe of the activated carbon adsorption system through the vacuum valve 47 and the vortex air pump 6;
the outlet duct of the third activated carbon adsorption tank 3 is divided into three paths: one path is discharged through a third discharge valve 34 and then communicated to the air inlet end at the bottom of the first activated carbon adsorption tank 1 through a first inlet valve 12, communicated to the air inlet end at the bottom of the second activated carbon adsorption tank 2 through a second inlet valve 22 and communicated to the air inlet end at the bottom of the third activated carbon adsorption tank 3 through a third inlet valve 32; one path is discharged through a third air outlet valve 35; one path is connected to the cooler 4 through a third drying valve 36, and is connected to an input pipe of the activated carbon adsorption system through a vacuum valve 47 and a vortex air pump 6;
the air outlet end of the cooler 4 is divided into two paths: one path is discharged through a condensing valve 43, and is communicated to the air inlet end at the bottom of the first activated carbon adsorption tank 1 through a first steam outlet valve 13, communicated to the air inlet end at the bottom of the second activated carbon adsorption tank 2 through a second steam outlet valve 23, and communicated to the air inlet end at the bottom of the third activated carbon adsorption tank 3 through a third steam outlet valve 33;
one path is communicated to the air inlet end of the fan 5 through an external drying valve 45; the air outlet end of the fan 5 is discharged through an internal drying valve 44; then respectively communicated to the air inlet end at the bottom of the first active carbon adsorption tank 1 through a first steam outlet valve 13, communicated to the air inlet end at the bottom of the second active carbon adsorption tank 2 through a second steam outlet valve 23, and communicated to the air inlet end at the bottom of the third active carbon adsorption tank 3 through a third steam outlet valve 33;
the liquid outlet end of the cooler 4 is connected to a separation tank 7 through a liquid outlet valve 46, and the separation tank 7 is connected to a metering tank 8 through a pipeline;
the separation tank 7 and the metering tank 8 are respectively communicated to the air inlet end of the vortex air pump 6 through an exhaust valve 48 and a vacuum valve 47;
the first activated carbon adsorption tank 1 is connected with a steam pipeline with a first steam inlet valve 17, the second activated carbon adsorption tank 2 is connected with a steam pipeline with a second steam inlet valve 27, and the third activated carbon adsorption tank 3 is connected with a steam pipeline with a third steam inlet valve 37;
the input pipe of the active carbon adsorption system is also connected with a pipeline with an air release valve 42.
Specifically, in a process flow of the present invention, a series flow is formed between the first activated carbon adsorption tank 1 and the second activated carbon adsorption tank 2 through the control of a pipeline and a valve, i.e. a first-stage and second-stage adsorption system is realized, organic waste gas passes through the tail gas main valve 41, enters the first activated carbon adsorption tank 1 through the first deflation valve 11, is discharged through the first discharge valve 14, enters the second activated carbon adsorption tank 2 through the second inlet valve 22, and is then discharged through the second outlet valve 25, such that the organic solvent in the organic waste gas is subjected to activated carbon adsorption treatment and then reaches the emission standard.
Simultaneously, the third activated carbon adsorption tank 3 begins to perform steam desorption: specifically, steam enters the third activated carbon adsorption tank 3 through the third steam inlet valve 37, steam desorption analysis is carried out on activated carbon in the third activated carbon adsorption tank 3, steam after analysis is discharged through the third steam outlet valve 33, the steam is condensed in the cooler 4 through the condensing valve 43, condensed condensate enters the separation tank 7 through the liquid discharge valve 46, and separated organic solvent enters the metering tank 8 through a pipeline and is recycled through the pipeline. Meanwhile, the air discharged from the cooler 4, the separation tank 7 and the metering tank 8 passes through the vacuum valve 47 and the exhaust valve 48, and is discharged to the tail gas total treatment through the vortex air pump 6.
When the steam desorption and analysis of the third activated carbon adsorption tank 3 are finished, vacuumizing is started: a small amount of aromatic hydrocarbon and steam in the third activated carbon adsorption tank 3 pass through a third steam outlet valve 33, a condensing valve 43, a cooler 4 for condensation and a vacuum valve 47, and are discharged to the tail gas total treatment through a vortex air pump 6; the condensate is discharged into the separation tank 7 through a drain valve.
Drying in a fan in a circulating manner: air enters the third activated carbon adsorption tank 3 through the fan 5, the inner drying valve 44 and the third steam outlet valve 33 for drying, is discharged from the third drying valve 36, is condensed through the cooler 4, returns to the inlet of the fan 5 through the outer drying valve 45 for internal circulation drying, and is discharged into the separation tank 7 through the liquid discharge valve.
Drying by external circulation of a fan: air enters the third activated carbon adsorption tank 3 through the fan 5, the inner drying valve 44 and the third steam outlet valve 33 for drying and cooling, and is discharged through the third air outlet valve 35.
After the third activated carbon adsorption tank 3 is dried and cooled, the second activated carbon adsorption tank 2 and the third activated carbon adsorption tank 3 form a series flow through the control of a pipeline and a valve, namely, a one-stage two-stage adsorption system is realized, organic waste gas enters the second activated carbon adsorption tank 2 through a second air release valve 21 and is discharged through a second discharge valve 24 until a third inlet valve 32 enters the third activated carbon adsorption tank 3, and then is discharged through a third air outlet valve 35. Meanwhile, the first activated carbon adsorption tank 1 starts to be subjected to steam desorption condensation, vacuum pumping, fan internal circulation drying and fan external circulation drying; the operation is circulated in such a way. The utility model discloses in, the active carbon adsorption jar that adsorbs organic solvent separates organic solvent through steam desorption analysis, condenser condensation, separating tank and retrieves, and analytic water leads to the sewage station and handles. Fig. 3 shows a flow chart of the adsorption and steam desorption condensation process of the activated carbon adsorption tank in the activated carbon adsorption system of the present invention.
In a specific embodiment of the utility model, the active carbon adsorption system is controlled by a DSC system, and is fully automatically monitored and controlled, and the DSC control system is set to be normally stopped, reset and suddenly stopped; the device is provided with a safety interlock system, an emergency emptying system and an emergency emptying system, and is capable of automatically circulating and operating, and simple and easy to operate.
Fig. 4 is a flow chart showing a vacuum-pumping and fan-drying process in the middle activated carbon adsorption system of the present invention, wherein the flow specifically includes three operation procedures of vacuum-pumping, fan internal circulation drying and fan external drying; because a large amount of water and a small amount of organic solvent steam remain in the activated carbon after each steam desorption, the adsorption effect of the activated carbon is seriously influenced; in addition, the temperature of the activated carbon after the steam desorption is generally more than 100 ℃, the adsorption effect of the activated carbon is also seriously influenced, therefore, in the utility model, after the activated carbon adsorption tank undergoes the steam desorption, the activated carbon adsorption tank is firstly vacuumized by the vortex air pump 6 through the cooler 4, part of the organic solvent steam is cooled and recovered, then the internal circulation drying is carried out through the cooler 4 by the fan 5, and further a large amount of residual moisture and a small amount of organic solvent steam in the activated carbon are circularly cooled, condensed and recovered; then air is sent in through a fan 5 to cool and dry the activated carbon adsorption tank.
In the utility model, the internal circulation drying of the fan is carried out before the external drying of the fan, thereby effectively preventing the problems that the external drying of the fan affects the emission detection data and the odor appears on site; through the final drying step outside the fan, the temperature is reduced to below 35 ℃ when organic waste gas is adsorbed in the next period, and the adsorption effect is ensured.
The utility model discloses in, the active carbon adsorption jar after the dry cooling of fan, form the series connection at absorbent active carbon adsorption jar with one of them and continue to circulate and use, and another active carbon adsorption jar carries out the steam desorption, so, realized the not shut down operation of active carbon adsorption system, improved organic waste gas's treatment effeciency.
The utility model provides an improvement method has realized that there is the effective processing of organizing and each storage tank unorganized atmospheric gas in anthraquinone process production hydrogen peroxide solution system, and this improvement method has degree of automation height, easy operation, and the running cost is low, and purification efficiency is high, safe advantage economic again promptly.
The foregoing shows and describes the general principles, essential features, and features of the invention. It should be understood by those skilled in the art that the present invention is not limited to the above embodiments, and the description of the above embodiments and the description is only illustrative of the principles of the present invention, and that various changes and modifications may be made without departing from the spirit and scope of the present invention, and these changes and modifications are all within the scope of the present invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (3)
1. An organic waste gas treatment system for producing hydrogen peroxide by an anthraquinone process is characterized by comprising a cooling condensation separation system and an active carbon adsorption system;
the cooling condensation separation system comprises a primary cooler, a primary separator, a secondary cooler and a secondary separator; cooling the organic waste gas to be treated by a first-stage cooler, separating by a first-stage separator, cooling by a second-stage cooler, and separating by a second-stage separator;
the active carbon adsorption system comprises at least three active carbon adsorption tanks, and a cooler, a separation tank, a metering tank, a fan, a vortex air pump, a control valve and a DCS control system which are matched with the active carbon adsorption tanks;
every two activated carbon adsorption tanks are connected through a valve and a pipeline to form a primary and secondary adsorption process, organic solvent in the organic waste gas is discharged after being adsorbed by the activated carbon adsorption tanks, the activated carbon adsorption tanks adsorbing the organic solvent are subjected to steam desorption, condenser condensation and separation tank separation to obtain the organic solvent for recovery, and the desorbed water is led to a sewage station for treatment.
2. The organic waste gas treatment system for producing hydrogen peroxide by an anthraquinone process according to claim 1, further comprising: the storage tank is in an unorganized discharge and recovery system,
the device comprises a pipeline, a cooler, a separation tank and a vortex air pump; the unorganized emptying gas of each storage tank passes through a pipeline, is cooled, condensed and separated by a cooler and a separating tank, and is pumped into the activated carbon adsorption system by a vortex gas pump for treatment.
3. The organic waste gas treatment system for producing hydrogen peroxide by an anthraquinone process according to claim 1, wherein the activated carbon adsorption system comprises three activated carbon adsorption tanks, namely a first activated carbon adsorption tank, a second activated carbon adsorption tank and a third activated carbon adsorption tank;
a tail gas main valve is arranged on an input pipe of the activated carbon adsorption system, and the other end of the tail gas main valve is connected to the air inlet end of the bottom of the first activated carbon adsorption tank through a first air release valve, connected to the air inlet end of the bottom of the second activated carbon adsorption tank through a second air release valve and connected to the air inlet end of the bottom of the third activated carbon adsorption tank through a third air release valve;
the outlet duct of first active carbon adsorption jar divide into three routes: one path is discharged through a first discharge valve and then is communicated to the air inlet end at the bottom of the first activated carbon adsorption tank through a first inlet valve, is communicated to the air inlet end at the bottom of the second activated carbon adsorption tank through a second inlet valve, and is communicated to the air inlet end at the bottom of the third activated carbon adsorption tank through a third inlet valve; one path is discharged through a first air outlet valve; one path of the air is connected to a cooler through a first drying valve, and is connected to an input pipe of the activated carbon adsorption system through a vacuum valve and a vortex air pump;
the outlet duct of second active carbon adsorption jar divide into three routes: one path is discharged through a second joint outlet valve and then is communicated to the air inlet end at the bottom of the first activated carbon adsorption tank through a first joint inlet valve, is communicated to the air inlet end at the bottom of the second activated carbon adsorption tank through the second joint inlet valve, and is communicated to the air inlet end at the bottom of the third activated carbon adsorption tank through a third joint inlet valve; one path is discharged through a second air outlet valve; one path of the air is connected to a cooler through a second drying valve, and is connected to an input pipe of the activated carbon adsorption system through a vacuum valve and a vortex air pump;
the outlet duct of the third activated carbon adsorption tank is divided into three paths: one path is discharged through a third discharge valve and then is communicated to the air inlet end at the bottom of the first activated carbon adsorption tank through a first joint inlet valve, is communicated to the air inlet end at the bottom of the second activated carbon adsorption tank through a second joint inlet valve, and is communicated to the air inlet end at the bottom of the third activated carbon adsorption tank through a third joint inlet valve; one path is discharged through a third air outlet valve; one path of the air is connected to a cooler through a third drying valve, and is connected to an input pipe of the activated carbon adsorption system through a vacuum valve and a vortex air pump;
the air outlet end of the cooler is divided into two paths: one path is discharged through a condensing valve, and is communicated to the air inlet end at the bottom of the first activated carbon adsorption tank through a first steam outlet valve, communicated to the air inlet end at the bottom of the second activated carbon adsorption tank through a second steam outlet valve, and communicated to the air inlet end at the bottom of the third activated carbon adsorption tank through a third steam outlet valve;
one path is communicated to the air inlet end of the fan through an external drying valve; the air outlet end of the fan is discharged through an inner drying valve; the first steam outlet valve is communicated with the air inlet end at the bottom of the first activated carbon adsorption tank, the second steam outlet valve is communicated with the air inlet end at the bottom of the second activated carbon adsorption tank, and the third steam outlet valve is communicated with the air inlet end at the bottom of the third activated carbon adsorption tank;
the liquid outlet end of the cooler is connected to a separation tank through a liquid discharge valve, and the separation tank is connected to a metering tank through a pipeline;
the separation groove and the metering groove are respectively communicated to the air inlet end of the vortex air pump through an exhaust valve and a vacuum valve;
the first activated carbon adsorption tank is connected with a steam pipeline with a first steam inlet valve, the second activated carbon adsorption tank is connected with a steam pipeline with a second steam inlet valve, and the third activated carbon adsorption tank is connected with a steam pipeline with a third steam inlet valve;
and the input pipe of the activated carbon adsorption system is also connected with a pipeline with an emptying valve.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202020473967.2U CN212327825U (en) | 2020-04-01 | 2020-04-01 | Organic waste gas treatment system for producing hydrogen peroxide by anthraquinone process |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111437690A (en) * | 2020-04-01 | 2020-07-24 | 安徽晋煤中能化工股份有限公司 | Organic waste gas treatment system for producing hydrogen peroxide by anthraquinone process |
| CN114797364A (en) * | 2022-05-07 | 2022-07-29 | 山东明化新材料有限公司 | Green production method and system for realizing carbon emission reduction by hydrogen peroxide tail gas self-circulation |
| CN117123019A (en) * | 2023-10-26 | 2023-11-28 | 天津渤化化工发展有限公司 | Method for treating hydrogen peroxide oxidation tail gas by anthraquinone process |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111437690A (en) * | 2020-04-01 | 2020-07-24 | 安徽晋煤中能化工股份有限公司 | Organic waste gas treatment system for producing hydrogen peroxide by anthraquinone process |
| CN114797364A (en) * | 2022-05-07 | 2022-07-29 | 山东明化新材料有限公司 | Green production method and system for realizing carbon emission reduction by hydrogen peroxide tail gas self-circulation |
| CN114797364B (en) * | 2022-05-07 | 2023-11-17 | 山东明化新材料有限公司 | Environment-friendly production method and system for realizing carbon emission reduction by hydrogen peroxide tail gas self-circulation |
| CN117123019A (en) * | 2023-10-26 | 2023-11-28 | 天津渤化化工发展有限公司 | Method for treating hydrogen peroxide oxidation tail gas by anthraquinone process |
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