CN109200735B - Method for treating hydrogen peroxide oxidized tail gas - Google Patents
Method for treating hydrogen peroxide oxidized tail gas Download PDFInfo
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- CN109200735B CN109200735B CN201710521454.7A CN201710521454A CN109200735B CN 109200735 B CN109200735 B CN 109200735B CN 201710521454 A CN201710521454 A CN 201710521454A CN 109200735 B CN109200735 B CN 109200735B
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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
- B01D53/002—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 condensation
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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
- B01D53/22—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 diffusion
- B01D53/228—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 diffusion characterised by specific membranes
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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
- B01D53/22—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 diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7027—Aromatic hydrocarbons
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
Abstract
A hydrogen peroxide oxidized tail gas treatment method comprises the steps of separating tail gas through a membrane separator, wherein a membrane in the membrane separator is a silicon rubber/poly-maple composite membrane, the aperture of the membrane is 0.01-1.0 um, the inner diameter of the membrane is 0.1-1.0 mm, and the wall thickness of the membrane is 0.5-1.5 mm; before use, the product is soaked in low carbon alcohol and treated with inert gas or nitrogen in three stages. The tail gas treatment method of the invention utilizes the special treated membrane separator, changes the permeation characteristic of the membrane, removes the micromolecule polymer impurities in the membrane component, makes the pore size distribution of the membrane component more uniform, and can effectively separate and recover the aromatic hydrocarbon component in the tail gas; the invention also has the advantages of low equipment investment cost, long service cycle, simple operation and low energy consumption.
Description
Technical Field
The invention relates to a method for treating tail gas in a hydrogen peroxide production process, and relates to a method for separating and recovering aromatic hydrocarbon in the tail gas.
Background
The tail gas from the anthraquinone process to produce hydrogen peroxide comes from an oxidation tower, and the aromatic hydrocarbon content in the tail gas reaches 20g/m after the tail gas is condensed (10-20 ℃)3-30g/m3. The aromatic hydrocarbon has strong volatility and is easy to run and damage along with gas phase, and the aromatic hydrocarbon belongs to benzene substances, so the environmental pollution is serious if the aromatic hydrocarbon is not recovered in time. The general treatment method is that the tail gas is firstly condensed by a heat exchanger to most of aromatic hydrocarbon gas, then the pressure of the oxidized tail gas is used as power, the temperature is cooled by an expansion unit, the heavy aromatic hydrocarbon in the tail gas is further condensed and recovered, and the heavy aromatic hydrocarbon is directly discharged after being adsorbed by activated carbon fibers.
Because the liquid drop diameter of the liquid aromatic hydrocarbon carried in the tail gas is very small, usually 1um-l0um, the common condensation-adsorption is adopted to adsorb the aromatic hydrocarbon in the tail gas, besides the gas aromatic hydrocarbon to be adsorbed, the aromatic hydrocarbon in the small drop form also needs to be adsorbed, thus greatly increasing the load of an adsorption device.
To understandIn order to solve the problems, patent CN1483503A discloses a method for purifying and recovering aromatic hydrocarbon in tail gas of a hydrogen peroxide production device, which adopts a pretreated activated carbon catalyst as an adsorbent to remove the aromatic hydrocarbon in the tail gas, and then uses superheated steam or N2Heating at 120-400 deg.c for desorption.
Patents CN106139824A and CN204550425A disclose a hydrogen peroxide oxidized tail gas recycling device, which comprises an absorption tower, a rich liquid tank, a stripping tower, a separator, a recovery tank, a rectifying tower and a refining tank, which are connected in sequence through pipelines; the device is also provided with a barren liquor tank, a discharge hole of the barren liquor tank is connected to the absorption tower, the stripping tower and the rectifying tower are provided with feed inlets which are connected to the barren liquor tank through pipelines, the top of the absorption tower is provided with an emptying pipeline, the top of the absorption tower is provided with an adsorption tank, and carbon fibers are filled in the adsorption tank.
In patent CN1973958A, it is described that two adsorption beds filled with adsorbent are used to alternately adsorb and desorb organic matters in tail gas, and the desorption gas uses compressed air or nitrogen to regenerate adsorbent, and then uses existing cooler, absorption tower, spray tower and other equipment to recover aromatic hydrocarbon.
Patent CN102008862A discloses a recovery device and a recovery method for aromatic hydrocarbon in tail gas in hydrogen peroxide production process, the method adopts a condensation mode to condense most of aromatic hydrocarbon, then adopts a gas-liquid removing device to remove aromatic hydrocarbon liquid drops in tail gas, and then further absorbs aromatic hydrocarbon by an adsorption device to reach relevant emission standards.
Patents CN106139789A and CN204543898A disclose a device for increasing recovery rate of aromatic hydrocarbons in hydrogen peroxide oxidized tail gas, which includes a first-stage condenser, an intermediate separation tank, a second-stage condenser, a cyclone separator, and an oil-water separator.
Patent CN202700289A discloses a device for treating tail gas generated by hydrogen peroxide oxidation, which comprises a tank body arranged outside a membrane filter, a tail gas inlet arranged on the left side edge of the lower part of the tank body, and a tail gas outlet arranged on the upper part of the tank body, wherein the tail gas inlet is used for collecting and filtering liquid drops in a gas state.
The tail gas treatment device mentioned in the above documents generally has the problems of high operating cost, complex flow, high energy consumption, unsatisfactory staticizing treatment effect and the like, so that aromatic hydrocarbons in the tail gas are fully recovered in a proper mode, the discharged tail gas is stably discharged up to the standard, and the tail gas treatment device has important significance for reducing the production cost and protecting the environment.
Disclosure of Invention
In order to solve the problems of complex treatment process, high cost and substandard tail gas treatment effect of a tail gas treatment method generated in the hydrogen peroxide production process in the prior art, the invention aims to provide the tail gas treatment method, which treats a membrane component by a specific means, and utilizes a membrane separator to separate and treat the tail gas, so that aromatic hydrocarbon in the tail gas is fully recovered, and the discharged tail gas reaches the standard.
In order to achieve the technical purpose, the invention adopts the following technical means:
the invention provides a method for treating hydrogen peroxide oxidized tail gas, which comprises the steps of condensing the tail gas to 5-30 ℃, introducing the tail gas into a membrane separator for membrane separation, recovering aromatic hydrocarbons in the tail gas, and purifying the tail gas;
wherein, the membrane in the membrane separator is a hollow fiber composite organic membrane, the aperture of the membrane is 0.01 um-1.0 um, the inner diameter is 0.1 mm-1.0 mm, and the wall thickness is 0.5 mm-1.5 mm;
the membrane reactor is treated before use by:
low carbon alcohol is first soaked at 50-200 deg.c for 4-24 hr and then inert gas or nitrogen is introduced in three stages at the pressure of 0.5-1.0 MPa, temperature of 50-80 deg.c and flow rate of 1m3/h-5m3H; the conditions of introducing inert gas or nitrogen in the second stage are that the pressure is 0.8MPa-1.0MPa, the temperature is 60-80 ℃, and the flow speed is 3m3/h-5m3H; the third stage is fed with inert gas or nitrogen under the conditions of pressure of 1.0MPa-1.5MPa, temperature of 90-100 deg.C and flow rate of 6m3/h-8m3/h。
In the above treatment method, it should be understood by those skilled in the art that the hydrogen peroxide oxidation tail gas refers to tail gas generated in an oxidation stage in the hydrogen peroxide production process by the anthraquinone process, mainly air and heavy aromatics, which cannot be directly discharged and needs to be recovered.
In the treatment method, the tail gas is more preferably condensed to 10-20 ℃.
In the above treatment method, the hollow fiber composite organic membrane is preferably a silicone rubber/polysulfone composite membrane. Further preferably, the membrane pore size is 0.01 to 0.6um, more preferably 0.01 to 0.4 um; the inner diameter is 0.2mm to 1.0mm, more preferably 0.2mm to 0.8 mm; the thickness of the film is 0.5mm to 1.0mm, more preferably 0.5mm to 0.8 mm.
In the above treatment method, as a further preferable mode, the lower alcohol is selected from C1-C7Preferably C, and at least one of normal alcohols and isomeric alcohols of1-C4More preferably C, and at least one of normal alcohols and isomeric alcohols of1-C3At least one of normal alcohols and isomeric alcohols.
In the above treatment method, as a further preference, the soaking condition using the lower alcohol is preferably a soaking condition at a temperature of 50 ℃ to 150 ℃ for 12 hours to 24 hours.
In the above treatment method, the soaking according to the present invention is based on the condition that the membrane module is completely submerged by the liquid.
In the treatment method, the membrane separator comprises a shell and a membrane component, the membrane component is arranged in the shell, a tail gas inlet is arranged at one end of the shell in parallel with the membrane component, a residual gas outlet is arranged at the other end of the shell in parallel with the membrane component, and an aromatic hydrocarbon outlet penetrating through the membrane is arranged on the side surface of the shell.
In the process of treating tail gas by the membrane separator, the tail gas flows in the membrane component, and aromatic hydrocarbon components permeating through the membrane flow out of the outer tube of the membrane component, so that the aromatic hydrocarbon components can be effectively recovered.
Compared with the prior art, the hydrogen peroxide oxidized tail gas treatment method has the following advantages:
1. the invention removes the micromolecule polymer impurities in the membrane component by soaking the membrane separator with low carbon alcohol under specific conditions and processing with inert gas or nitrogen in stages, so that the pore size distribution of the membrane component is more uniform, and the enrichment of aromatic hydrocarbon components is more facilitated.
2. Compared with other processes, the hydrogen peroxide oxidized tail gas treatment method has the advantages of low equipment investment cost, long service cycle, simple operation and low energy consumption; the membrane separator after special treatment has good separation selectivity and high separation efficiency, effectively recovers the aromatic hydrocarbon components in the tail gas, has the recovery efficiency 2 percent higher than that of a module without treatment, realizes more effective recovery of the aromatic hydrocarbon components, and does not generate secondary pollution in the whole process.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
FIG. 1 is a flow chart of a specific process for treating hydrogen peroxide oxidation tail gas used in the example;
FIG. 2 is a schematic structural view of a membrane separator;
the system comprises a first-stage condenser, a membrane separator, a water-oil separator, a valve I, a valve II, a purified tail gas outlet, a shell, a membrane assembly, a tail gas inlet and an aromatic hydrocarbon outlet, wherein the first-stage condenser is 1, the membrane separator is 2, the oil-water separator is 3, the valve I and the valve II are 5, the valve II and the valve 21 are 21, the purified tail gas outlet is.
Detailed Description
The following non-limiting examples are presented to enable those of ordinary skill in the art to more fully understand the present invention and are not intended to limit the invention in any way.
In the following embodiments, the process flow apparatus shown in fig. 1 is used to treat the hydrogen peroxide oxidation tail gas, as shown in fig. 1 and 2, the tail gas is condensed to 5 ℃ to 30 ℃ by the first-stage condenser 1, enters the lower part of the membrane separator 2 from the tail gas inlet 24 through the valve i 4, the membrane separator has a housing 22, a membrane module 23 is arranged in the housing, a tail gas inlet 24 is arranged at one end of the housing 22 in parallel with the membrane module 23, a purified tail gas outlet 21 is arranged at the other end of the housing 22 in parallel with the membrane module 23, and an aromatic hydrocarbon outlet 25 is arranged on the side surface of the. The hydrogen peroxide oxidized tail gas flows in the membrane component 23, is purified by the membrane, is directly discharged through the purified tail gas outlet 21, and the aromatic hydrocarbon components penetrating through the membrane flow out of the membrane component, are discharged through the aromatic hydrocarbon outlet 25 and enter the oil-water separator 3. The oil-water separator 3 is internally provided with a clapboard for separating the aromatic hydrocarbon which can be recycled.
The film parameters used in the examples are shown in table 1.
TABLE 1
Example 1
Before introducing tail gas, the membrane component is soaked in isopropanol solvent at 50 deg.C for 12 hr, and then nitrogen gas is introduced in three stages under the conditions of 0.5MPa pressure, 80 deg.C temperature and 5m flow rate3H; the second stage is fed with nitrogen under the conditions of 0.8MPa of pressure, 60 ℃ of temperature and 3m of flow speed3H; the nitrogen is introduced into the third stage under the conditions of 1.5MPa of pressure, 100 ℃ of temperature and 8m of flow speed3And h, purifying the hydrogen peroxide oxidized tail gas after the treatment is finished. The tail gas is condensed to 10 ℃, 10 hydrogen peroxide oxidized tail gases with different aromatic hydrocarbon contents, which are numbered 1-10, are treated by adopting the process flow shown in figure 1, and the results are shown in table 2.
Example 2
The procedure of example 1 was followed except that isopropanol was changed to ethanol, and the results are shown in Table 2.
Example 3
The procedure of example 1 was followed except that isopropanol was changed to n-butanol, and the results are shown in Table 2.
Example 4
The procedure of example 1 was followed except that isopropanol was changed to octanol, and the results are shown in Table 2.
Example 5
According to the method of example 1, the following treatment was carried out on the hollow fiber composite organic membrane module before the introduction of the tail gas: soaking the membrane module in ethanol solvent at 80 deg.C for 12h, introducing nitrogen gas in three stages, wherein the nitrogen gas is introduced at 80 deg.C under 1.0MPa in the first stage and at flow rate of 5m3H; the second stage is fed with nitrogen under the conditions of 0.8MPa of pressure, 60 ℃ of temperature and 3m of flow speed3H; the nitrogen is introduced into the reactor at 100 deg.C under 1.5MPa and 6m3And h, purifying the hydrogen peroxide oxidized tail gas after the treatment is finished. The results are shown in Table 2.
Example 6
The procedure of example 1 was followed except that ethanol was changed to sec-butanol, and the results are shown in Table 2.
Example 7
The procedure of example 1 was followed except that ethanol was changed to methanol, and the results are shown in Table 2.
Example 8
According to the method of example 1, the following treatment was carried out on the hollow fiber composite organic membrane module before the introduction of the tail gas: soaking the membrane component in methanol solvent at 50 deg.C for 24h, introducing nitrogen gas in three stages, wherein the nitrogen gas is introduced at the first stage under the conditions of 1.0MPa, 80 deg.C and 5m flow rate3H; the second stage is fed with nitrogen under the conditions of pressure of 0.8MPa, temperature of 80 deg.C and flow rate of 3m3H; the nitrogen is introduced into the third stage under the conditions of 1.5MPa of pressure, 100 ℃ of temperature and 8m of flow speed3And h, purifying the hydrogen peroxide oxidized tail gas after the treatment is finished. The results are shown in Table 2.
Example 9
The procedure of example 10 was followed except that methanol was changed to ethanol, and the results are shown in Table 2.
Example 10
The procedure of example 10 was followed except that methanol was changed to isopropanol, and the results are shown in Table 2.
Example 11
The procedure of example 10 was followed except that methanol was changed to butanol, and the results are shown in Table 2.
Comparative example 1
According to the method disclosed by the patent CN202700289U, 10 hydrogen peroxide oxidized tail gases with different aromatic hydrocarbon contents, which are numbered 1-10, are treated, and the results are shown in a table 2.
As can be seen from Table 2, the hydrogen peroxide oxidized tail gas is treated by adopting the membrane filter which is not pretreated in the comparative example, while the membrane separator is specially treated in the method of the invention, the content of aromatic hydrocarbon components in the tail gas treated by the method of the invention is reduced by at least about 2 percent compared with the method of the comparative example from the treatment result, and the more effective recovery of the aromatic hydrocarbon components is realized.
Claims (7)
1. A method for treating tail gas oxidized by hydrogen peroxide comprises the steps of condensing the tail gas to 5-30 ℃, introducing the tail gas into a membrane separator for membrane separation, recovering aromatic hydrocarbons in the tail gas, and purifying the tail gas;
wherein, the membrane in the membrane separator is a hollow fiber composite organic membrane, in particular to a silicon rubber/polysulfone composite membrane, the aperture of the membrane is 0.01-0.4 μm, the inner diameter is 0.1-1.0 mm, and the wall thickness is 0.5-1.5 mm;
the membrane separator is treated prior to use by:
low carbon alcohol is first soaked at 50-200 deg.c for 4-24 hr and then inert gas or nitrogen is introduced in three stages at the pressure of 0.5-1.0 MPa, temperature of 50-80 deg.c and flow rate of 1m3/h-5m3H; the conditions of introducing inert gas or nitrogen in the second stage are that the pressure is 0.8MPa-1.0MPa, the temperature is 60-80 ℃, and the flow speed is 3m3/h-5m3H; the third stage is fed with inert gas or nitrogen under the conditions of pressure of 1.0MPa-1.5MPa, temperature of 90-100 deg.C and flow rate of 6m3/h-8m3/h。
2. The process of claim 1, wherein the off-gas is condensed to 10 ℃ to 20 ℃.
3. The method according to claim 1, wherein the silicone rubber/polysulfone composite membrane has an inner diameter of 0.2mm to 1.0mm and a wall thickness of 0.5mm to 1.0 mm.
4. The method according to claim 3, wherein the silicone rubber/polysulfone composite membrane has an inner diameter of 0.2mm to 0.8mm and a wall thickness of 0.5mm to 0.8 mm.
5. The process according to claim 1, characterized in that the lower alcohol is selected from C1-C7At least one of normal alcohols and isomeric alcohols.
6. The process according to claim 5, characterized in that the lower alcohol is selected from C1-C4At least one of normal alcohols and isomeric alcohols.
7. The treatment method according to claim 3, wherein the soaking with the lower alcohol is carried out at a temperature of 50 ℃ to 150 ℃ for 12 hours to 24 hours.
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| US6179996B1 (en) * | 1998-05-22 | 2001-01-30 | Membrane Technology And Research, Inc. | Selective purge for hydrogenation reactor recycle loop |
| CN1425486A (en) * | 2002-06-25 | 2003-06-25 | 南化集团研究院 | Recovery technology for volatile organism in mixed gas |
| CN202700289U (en) * | 2012-01-19 | 2013-01-30 | 江苏理文化工有限公司 | Device for processing hydrogen peroxide oxidation tail gas |
| CN205164447U (en) * | 2015-11-30 | 2016-04-20 | 青岛德尔通用环保科技有限公司 | Organic waste gas recovery device |
| CN105585417A (en) * | 2014-10-23 | 2016-05-18 | 中国石油化工股份有限公司 | Method for producing ethyl benzene from exhaust gas of polyethylene device |
| CN206081719U (en) * | 2016-10-19 | 2017-04-12 | 华南师范大学 | An organic waste gas purifier |
| CN106673962A (en) * | 2015-11-09 | 2017-05-17 | 中国石油化工股份有限公司 | Preparation method of isopropanol |
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2017
- 2017-06-30 CN CN201710521454.7A patent/CN109200735B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6179996B1 (en) * | 1998-05-22 | 2001-01-30 | Membrane Technology And Research, Inc. | Selective purge for hydrogenation reactor recycle loop |
| CN1425486A (en) * | 2002-06-25 | 2003-06-25 | 南化集团研究院 | Recovery technology for volatile organism in mixed gas |
| CN202700289U (en) * | 2012-01-19 | 2013-01-30 | 江苏理文化工有限公司 | Device for processing hydrogen peroxide oxidation tail gas |
| CN105585417A (en) * | 2014-10-23 | 2016-05-18 | 中国石油化工股份有限公司 | Method for producing ethyl benzene from exhaust gas of polyethylene device |
| CN106673962A (en) * | 2015-11-09 | 2017-05-17 | 中国石油化工股份有限公司 | Preparation method of isopropanol |
| CN205164447U (en) * | 2015-11-30 | 2016-04-20 | 青岛德尔通用环保科技有限公司 | Organic waste gas recovery device |
| CN206081719U (en) * | 2016-10-19 | 2017-04-12 | 华南师范大学 | An organic waste gas purifier |
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