CN106000012A - Efficient energy-saving recovery process and device for different concentrations of high-temperature tail gas - Google Patents
Efficient energy-saving recovery process and device for different concentrations of high-temperature tail gas Download PDFInfo
- Publication number
- CN106000012A CN106000012A CN201610610661.5A CN201610610661A CN106000012A CN 106000012 A CN106000012 A CN 106000012A CN 201610610661 A CN201610610661 A CN 201610610661A CN 106000012 A CN106000012 A CN 106000012A
- Authority
- CN
- China
- Prior art keywords
- concentration
- tail gas
- tower
- absorption
- absorption tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D53/1487—Removing organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
-
- 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
- B01D2257/704—Solvents not covered by groups B01D2257/702 - B01D2257/7027
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to an efficient energy-saving recovery process and device for different concentrations of high-temperature tail gas, belonging to the technical field of chemical engineering and petrifaction. According to the recovery process, heat is absorbed in a direct sectional manner by virtue of evaporation, low-concentration gas enters a lower-concentration absorption tower and is prepared into dilute liquid, and the dilute liquid enters a high-concentration absorption tower and is prepared into high-concentration absorption liquid by virtue of spray absorption. Compared with the prior art, the recovery process utilizing the technique has the advantages that a front tower cooler, a condenser and a separation tank are saved, the energy-saving effect is remarkable, the consumption of circulating water is reduced by 90%, low-temperature water is not required, the concentration of the absorption liquid reaches 49%, the energy consumption of subsequent rectification is greatly reduced, and the recovery process has remarkable economic and environmental benefits. By virtue of the recovery process, the consumption of circulating water and low-temperature water can be remarkably reduced, and the absorption liquid with a relatively high concentration can be prepared.
Description
Technical field
The invention belongs to chemical industry and petrochemical technology field, be specifically related to a kind of consumption that can reduce recirculated water, water at low temperature, and
And the energy-efficient recovery process of the high-temperature tail gas containing variable concentrations and the device thereof of the absorbing liquid of higher concentration can be made.
Background technology
Using absorption process to reclaim active component in emission is a kind of common chemical engineering unit operation, absorbing liquid
Concentration depend primarily on tail gas concentration, the equilibrium concentration of the highest then absorbing liquid of tail gas concentration is the biggest, the actual absorption of absorbing liquid
Concentration is the biggest.
In chemical process, can produce the high-temperature tail gas of various concentration, common technique is by the height of various concentration
After warm tail gas mixing, carry out cooling condensation and reclaim active component, then entering absorption tower absorption or the height to variable concentrations
Temperature tail gas individually condenses to enter absorption tower the most again and absorb.For low concentration tail gas, directly condensation is used to can only obtain low dense
The recovered liquid of degree, and for high concentration tail gas, use directly condensation can obtain the recovered liquid of higher concentration (with air humidity also phase
Closing, air humidity is the lowest, and the recovered liquid concentration obtained is the highest), and low due to air inlet active component concentration in follow-up absorption tower
(through condensed absorbent), therefore at the bottom of tower, absorbing liquid concentration just ratio is relatively low.Different according to active component boiling point, condensation segment needs to disappear
Consume other coolant such as a large amount of recirculated water, water at low temperature.The consumption of tradition recovery scheme coolant is big, and recovered liquid concentration is the highest.
Summary of the invention
For the above-mentioned problems in the prior art, it is desirable to provide a kind of high-temperature tail gas containing variable concentrations is high
Effect energy-saving reclaiming process and device thereof.
Described a kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations, it is characterised in that by direct segmentation
Formula absorbs, and utilizes evaporation to absorb heat, and light concentration gas enters lower concentration absorbing tower and makes thin liquid, and thin liquid enters high-concentration absorbent
Tower carries out spray-absorption again, makes the absorbing liquid of high concentration.
Described a kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations, it is characterised in that specifically include as follows
Step:
1) high-temperature tail gas is carried out segmentation by concentration, by the high-temperature tail gas of variable concentrations section successively by suitable from low concentration to high concentration
Sequence enters in corresponding absorption tower, absorbs with fresh soft water；
2) circulation in each absorption tower is connected formation with circulating pump, heat exchanger, thin liquid portion after absorption out bottom absorption tower
Divide and return absorption tower formation circulation, in the middle part of adjacent high-concentration absorbent tower after the absorption of extraction section thin liquid and lower concentration absorbing tower
Thin liquid mixes, and after heat exchanger heat exchange, enters back into high-concentration absorbent tower and carries out spray-absorption, finally obtain the absorption of high concentration
Liquid.
Described a kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations, it is characterised in that energy in high-temperature tail gas
The active component reclaimed is that polarity is high, and volatility is little, boiling point is high and dissolves each other in water or material that dissolubility is bigger.
Described a kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations, it is characterised in that energy in high-temperature tail gas
The active component reclaimed is amine, alcohols, ketone or acids.
Described a kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations, it is characterised in that energy in high-temperature tail gas
The active component reclaimed is selected from Methanamide, DMAC, ethylene glycol, propylene glycol, acetic acid, propanoic acid, dimethyl sulfoxide or N-methylpyrrole
Alkanone.
Described a kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations, it is characterised in that after absorption thin liquid from
The middle and upper part on absorption tower is back to absorption tower.
The described energy-efficient retracting device of the high-temperature tail gas containing variable concentrations, it is characterised in that include multiple absorption tower,
The most each absorption tower process tail gas concentration gradually rise, connect respectively bottom each absorption tower circulating pump and
Heat exchanger, is provided with mixed liquor storage tank between adjacent two absorption towers, is provided with heat exchanger, high temperature between mixed liquor storage tank and absorption tower
Tail gas is pressed concentration and is entered from bottom, absorption tower, and fresh soft water enters from top, absorption tower, and heat exchanger discharging opening is divided into two-way,
One tunnel is circulated in being formed in being back to absorption tower, and another road flows into mixed liquor storage tank, from the beginning of second absorption tower, each absorption
Arranging liquid outlet in the middle part of tower, the absorbing liquid that liquid outlet is extracted out delivers to mixed liquor storage tank, with the absorption of previous heat exchanger discharging opening
Liquid mixes, and entrance is drawn out of the middle and upper part, absorption tower of absorbing liquid and sprays, and the tail gas after process is discharged from top, absorption tower.
The described energy-efficient retracting device of the high-temperature tail gas containing variable concentrations, it is characterised in that the suction of heat exchanger discharging opening
Receive the liquid entrance absorption tower, middle and upper part from absorption tower.
The described energy-efficient retracting device of the high-temperature tail gas containing variable concentrations, it is characterised in that on last absorption tower
Portion is tower plate structure, and bottom is filling-material structure, and upper strata fresh water is absorbed as column plate and absorbs, and remaining backflow and circulation fluid are filler
Absorb.
By using above-mentioned technology, compared with prior art, beneficial effects of the present invention is as follows:
1) technique that the present invention provides, utilizes fresh water spray vaporization to reduce the temperature of feeding gas, low concentration heat exchanger, highly concentrated
Degree heat exchanger and mixed liquor heat exchanger primarily serve the purpose of the Temperature Distribution of stable absorption tower, remove after-heat, only use recirculated water
?.Recirculated water consumption is relevant to ambient humidity.Ambient humidity more systemic circulation water usage amount is the biggest, the wettest with when 40 DEG C 70%
Degree charging calculates, and this technique can save the recirculated water of about 90%, it is not necessary to water at low temperature；
2) the high-concentration absorbent tower upper strata fresh water of the present invention is absorbed as column plate absorption, remaining backflow and circulation fluid is that filler is inhaled
Receive, not only ensure that absorption efficiency but also decrease energy consumption；
3) present invention is by absorbent components, the analysis of existing procedure, it is proposed that directly stagewise absorption process, energy-efficient recovery
Active component in high-temperature tail gas containing variable concentrations, makes the tail gas of last high-concentration absorbent tower higher concentration to be processed,
Compared with the prior art, present invention saves cooler before tower, condenser and knockout drum, its energy-saving effect is notable, and recirculated water consumes
Measure reduction by 90%, it is not necessary to water at low temperature, and absorbing liquid concentration reaches 49%, greatly alleviates the energy consumption of follow-up distillation operation, has aobvious
Write ground economic benefit and environmental benefit.
Accompanying drawing explanation
Fig. 1 is the structural representation of the embodiment of the present invention.
In figure: 1-lower concentration absorbing tower, 2-low concentration circulating pump, 3-low concentration heat exchanger, 4-mixed liquor storage tank, 5-mixes
Liquid circulating pump, 6-high-concentration absorbent tower, 7-high concentration heat exchanger, 8-high concentration circulating pump, 9-mixed liquor heat exchanger.
Detailed description of the invention
Below in conjunction with Figure of description and embodiment, the invention will be further described, but protection scope of the present invention is also
It is not limited only to this:
As it is shown in figure 1, the energy-efficient retracting device of the high-temperature tail gas containing variable concentrations of the present invention, including multiple absorption towers, press
The tail gas concentration that the most each absorption tower of order processes gradually rises, and last top, absorption tower is tower plate structure, under
Portion is filling-material structure, and upper strata fresh water is absorbed as column plate and absorbs, and remaining backflow and circulation fluid are packing material absorbing；Each absorption tower
Bottom connects circulating pump and heat exchanger respectively, is provided with mixed liquor storage tank, mixed liquor storage tank and absorption between adjacent two absorption towers
Being provided with heat exchanger between tower, high-temperature tail gas is pressed concentration and is entered from bottom, absorption tower, and fresh soft water enters from top, absorption tower,
Heat exchanger discharging opening is divided into two-way, and a road is circulated in being formed in being back to absorption tower, and another road flows into mixed liquor storage tank, from second
Individual absorption tower starts, and arranges liquid outlet in the middle part of each absorption tower, and the absorbing liquid that liquid outlet is extracted out delivers to mixed liquor storage tank, with previous
The absorbing liquid mixing of individual heat exchanger discharging opening, entrance is drawn out of the middle and upper part, absorption tower of absorbing liquid and sprays, the tail gas after process
Discharge from top, absorption tower.
As it is shown in figure 1, process in the embodiment of the present invention is the tail gas of two kinds of variable concentrations, it is divided into low concentration tail gas and height
Concentration tail gas, the most also has two absorption towers, lower concentration absorbing tower 1 and high-concentration absorbent tower 6, goes out bottom lower concentration absorbing tower 1
Mouth is sequentially connected with low concentration circulating pump 2 and low concentration heat exchanger 3, and low concentration heat exchanger 3 liquid outlet is divided into two-way, and a road returns low
Concentration absorption tower 1 middle and upper part also forms interior circulation, and high-concentration absorbent tower 6 outlet at bottom is sequentially connected with high concentration circulating pump 8 and height
Concentration heat exchanger 7 also forms interior circulation, lower concentration absorbing tower 1
And between high-concentration absorbent tower 6, it being provided with mixed liquor storage tank 4, mixed liquor storage tank 4 liquid outlet is connected by mixed liquor circulating pump 5
High-concentration absorbent tower 6, mixed liquor storage tank 4 has two inlets, and one of them inlet connects another road of low concentration heat exchanger 3
Liquid outlet, another inlet connects liquid outlet in the middle part of high-concentration absorbent tower 6, is provided with low concentration tail bottom lower concentration absorbing tower 1
Gas import, top is provided with low concentration exhaust port after fresh soft water import and process, is provided with highly concentrated bottom high-concentration absorbent tower 6
Degree inlet exhaust gas, top is provided with high concentration exhaust port after fresh soft water import and process, and the circulation fluid on two absorption towers enters
Mouthful being all disposed within middle and upper part, absorption tower, and be positioned at fresh soft water import, the waste gas being on the one hand avoided that in absorbing liquid is by gas band
On the other hand go out, GAS ABSORPTION amount can be increased, improve its concentration, bottom lower concentration absorbing tower 1 out partially absorb liquid with high
After the absorbing liquid extracted out in the middle part of concentration absorption tower 6 mixes in mixed liquor storage tank 4, mixed liquor circulating pump 5 pump into mixed liquor and change
After the heat exchange of hot device 9, being back to again in high-concentration absorbent tower 6, spray-absorption, the effective ingredient increased further in gases is inhaled
Receipts amount, thus obtain the absorbing liquid of high concentration, in two absorbing tower top row venting, effective ingredient reaches discharge standard.
The technique that the embodiment of the present invention provides, active component is as a example by dimethyl acetylamide (DMAC), with fresh water to two
The DMAC tail gas planting concentration absorbs, and in high concentration tail gas, DMAC content is 0.568%, and temperature is 85 DEG C, flow 105000
m3/ h, in low concentration tail gas, DMAC content is 0.117%, and temperature is 140 DEG C, flow 58700 m3/h。
The technique that the present invention provides, uses technique as shown in Figure 1, and low concentration tail gas enters lower concentration absorbing tower 1, high concentration
Tail gas enters high-concentration absorbent tower 6, and in discharge gas, DMAC reaches discharge standard, and relief liquor DMAC concentration theory can reach
More than 60%, it is considered to the problems such as economy, absorption tower efficiency, this technique optimal absorption liquid concentration is about 30% ~ 50%.
The technique that the present invention provides, utilizes fresh water spray vaporization to reduce the temperature of feeding gas, low concentration heat exchanger, height
Concentration heat exchanger and mixed liquor heat exchanger primarily serve the purpose of the Temperature Distribution of stable absorption tower, remove after-heat, only with circulation
Water.Recirculated water consumption is relevant to ambient humidity.Ambient humidity more systemic circulation water usage amount is the biggest, relative with when 40 DEG C 70%
Humidity charging calculates, and this technique can save the recirculated water of about 90%, it is not necessary to water at low temperature.
The technique that the present invention provides, it is contemplated that the key elements such as plate pressure drop, filler wettability power, absorbing liquid concentration, high concentration is inhaled
Receive tower 6 upper strata fresh water and be absorbed as that column plate absorbs, remaining backflow and circulation fluid are packing material absorbing, not only ensure that absorption efficiency but also
Decrease energy consumption.
The technique that the present invention provides, as more in variable concentrations tail gas quantity, tail gas that such as three kinds of concentration difference are bigger, can
Increasing a middle concentration absorption tower, auxiliary device is the same with lower concentration absorbing tower 1, in formation after concentration thin liquid, enters high concentration
The suitable feed entrance point in absorption tower 6.The thin liquid formed or middle thin liquid etc. all should enter the appropriate location of high-concentration absorbent tower 6, with this
Form high-concentration absorbent liquid.
Embodiment 1
Absorbent components is dimethyl acetylamide (DMAC), absorbs the DMAC tail gas of two kinds of concentration with fresh water, two kinds of tails
Gas composition is as follows:
Tail gas II is first condensed to 35 DEG C by traditional handicraft, the DMAC of about 80% during DMAC content is about 39%(tail gas II in condensed fluid
It is condensed to liquid), recirculated water 312t/h, water at low temperature 130t/h need to be consumed；Tail gas I condenses to 35 DEG C, and in condensed fluid, DMAC contains
Amount is about the DMAC of about 66% in 15%(tail gas II and is condensed to liquid), recirculated water 300t/h, water at low temperature 40t/h need to be consumed.Cold
Entering absorption tower after tail gas I after Ning and tail gas II mixing, absorbing liquid concentration is about about 10%, total condensed absorbent liquid concentration
About 28%, global cycle water consumption 612t/h, water at low temperature 170t/h.
Using direct stagewise absorption technique, tail gas I, at lower concentration absorbing tower cooling spray-absorption, obtains about 5% at the bottom of tower
DMAC thin liquid, overhead gas qualified discharge, tail gas II enter high-concentration absorbent tower carry out lower the temperature spray-absorption, middle part backflow
Return to middle and upper part after mixing with the DMAC thin liquid at the bottom of lower concentration absorbing tower tower, at the bottom of tower, obtain the DMAC absorbing liquid of 49%, tower overhead gas
Body qualified discharge.Recirculated water consumption about 60t/h, it is not necessary to water at low temperature.
The tail gas of high-concentration absorbent tower higher concentration to be processed, therefore the more former technique of tower height is high, but new technology saves tower
Front cooler, condenser and knockout drum, total equipment investment is the most suitable with former technique.This energy saving technology effect is notable, circulation
Water consumption reduces by 90%, it is not necessary to water at low temperature, and absorbing liquid concentration reaches 49%, greatly alleviates the energy consumption of follow-up distillation operation, tool
There are economic benefit and environmental benefit significantly.
Embodiment 2
Absorbent components is ethylene glycol (EG), absorbs the EG tail gas of two kinds of concentration with fresh water, and two kinds of tail gas compositions are as follows:
Owing to EG boiling point is higher, therefore condensing and only need recirculated water, be cooled to 40 DEG C, in condensed fluid, EG content is about 38.5%
(in tail gas I, the EG of about 93% is condensed to liquid), need to consume recirculated water 40t/h,；Tail gas II condenses to 40 DEG C, EG in condensed fluid
In content about 51%(tail gas II, the EG of about 95% is condensed to liquid), recirculated water 60t/h need to be consumed.Condensed tail gas I He
Entering absorption tower after tail gas II mixing, absorbing liquid concentration is below 5%, and because EG boiling point is high, the condensation response rate is high, should be with recovery
Liquid mix, the EG content so obtained about 46%, global cycle water consumption 100t/h.
Using direct stagewise absorption technique, tail gas I, at lower concentration absorbing tower cooling spray-absorption, obtains 10% left at the bottom of tower
Right EG thin liquid, overhead gas qualified discharge, tail gas II enters high-concentration absorbent tower and carries out spray-absorption of lowering the temperature, middle part backflow
Returning to middle and upper part after mixing with the EG thin liquid at the bottom of lower concentration absorbing tower tower, obtain the EG absorbing liquid of 62% at the bottom of tower, overhead gas reaches
Mark discharge.Recirculated water consumption about 4t/h.
Embodiment 3
Absorbent components is propanoic acid, absorbs the propanoic acid tail gas of two kinds of concentration with fresh water, and two kinds of tail gas compositions are as follows:
Condensing tail gas I to 30 DEG C, in condensed fluid, in DMAC content about 36.4%(tail gas II, the propanoic acid of about 77% is condensed to liquid
Body), recirculated water 330t/h, water at low temperature 240t/h need to be consumed；Tail gas II condenses to 30 DEG C, and in condensed fluid, DMAC content is about
In 17.4%(tail gas II, the propanoic acid of about 72% is condensed to liquid), recirculated water 287t/h, water at low temperature 330t/h need to be consumed.After condensation
Tail gas I and tail gas II mixing after enter absorption tower, absorbing liquid concentration is about about 8%, and total condensed absorbent liquid concentration is 27%
Left and right, global cycle water consumption 612t/h, water at low temperature 170t/h.
Using direct stagewise absorption technique, tail gas I, at lower concentration absorbing tower cooling spray-absorption, obtains about 8% at the bottom of tower
Propanoic acid thin liquid, overhead gas qualified discharge, tail gas II enter high-concentration absorbent tower carry out lower the temperature spray-absorption, middle part backflow
Return to middle and upper part after mixing with the propanoic acid thin liquid at the bottom of lower concentration absorbing tower tower, at the bottom of tower, obtain the propanoic acid absorbing liquid of 47.6%, tower overhead gas
Body qualified discharge.Recirculated water consumption about 1t/h, it is not necessary to water at low temperature.
Above-described three embodiments are only wherein three examples of the present invention, every relate to the multiple suction of polarity
The high-temperature tail gas receiving concentration of component absorbs, and can recycle with present invention process.
Claims (9)
1. the energy-efficient recovery process of high-temperature tail gas containing variable concentrations, it is characterised in that absorbed by direct stagewise,
Utilizing evaporation to absorb heat, light concentration gas enters lower concentration absorbing tower and makes thin liquid, and thin liquid enters high-concentration absorbent tower to be carried out
Spray-absorption again, makes the absorbing liquid of high concentration.
A kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations the most according to claim 1, it is characterised in that
Specifically include following steps:
1) high-temperature tail gas is carried out segmentation by concentration, by the high-temperature tail gas of variable concentrations section successively by suitable from low concentration to high concentration
Sequence enters in corresponding absorption tower, absorbs with fresh soft water；
2) circulation in each absorption tower is connected formation with circulating pump, heat exchanger, thin liquid portion after absorption out bottom absorption tower
Divide and return absorption tower formation circulation, in the middle part of adjacent high-concentration absorbent tower after the absorption of extraction section thin liquid and lower concentration absorbing tower
Thin liquid mixes, and after heat exchanger heat exchange, enters back into high-concentration absorbent tower and carries out spray-absorption, finally obtain the absorption of high concentration
Liquid.
A kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations the most according to claim 1 and 2, its feature exists
In high-temperature tail gas, recoverable active component is that polarity is high, and volatility is little, boiling point is high and dissolves each other in water or dissolubility is bigger
Material.
A kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations the most according to claim 3, it is characterised in that
In high-temperature tail gas, recoverable active component is amine, alcohols, ketone or acids.
A kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations the most according to claim 4, it is characterised in that
In high-temperature tail gas, recoverable active component is selected from Methanamide, DMAC, ethylene glycol, propylene glycol, acetic acid, propanoic acid, dimethyl sulfoxide
Or N-Methyl pyrrolidone.
A kind of energy-efficient recovery process of the high-temperature tail gas containing variable concentrations the most according to claim 2, it is characterised in that
After absorption, thin liquid is back to absorption tower from the middle and upper part on absorption tower.
7. the energy-efficient retracting device of the high-temperature tail gas containing variable concentrations according to claim 1, it is characterised in that
Including multiple absorption towers, the tail gas concentration that the most each absorption tower processes gradually rises, bottom each absorption tower
Connect circulating pump and heat exchanger respectively, between adjacent two absorption towers, be provided with mixed liquor storage tank, mixed liquor storage tank and absorption tower it
Between be provided with heat exchanger, high-temperature tail gas press concentration from bottom, absorption tower enter, fresh soft water from top, absorption tower enter, heat exchange
Device discharging opening is divided into two-way, and a road is circulated in being formed in being back to absorption tower, and another road flows into mixed liquor storage tank, from second suction
Receipts tower starts, and arranges liquid outlet in the middle part of each absorption tower, and the absorbing liquid that liquid outlet is extracted out delivers to mixed liquor storage tank, changes with previous
The absorbing liquid mixing of hot device discharging opening, entrance is drawn out of the middle and upper part, absorption tower of absorbing liquid and sprays, and the tail gas after process is from suction
Receipts top of tower is discharged.
The energy-efficient retracting device of high-temperature tail gas containing variable concentrations the most according to claim 7, it is characterised in that heat exchange
The absorbing liquid of device discharging opening is from the entrance absorption tower, middle and upper part on absorption tower.
The energy-efficient retracting device of high-temperature tail gas containing variable concentrations the most according to claim 7, it is characterised in that last
Top, one absorption tower is tower plate structure, and bottom is filling-material structure, upper strata fresh water be absorbed as column plate absorb, remaining backflow and
Circulation fluid is packing material absorbing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610610661.5A CN106000012B (en) | 2016-07-29 | 2016-07-29 | A kind of energy-efficient recovery process of high-temperature tail gas containing various concentration and its device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610610661.5A CN106000012B (en) | 2016-07-29 | 2016-07-29 | A kind of energy-efficient recovery process of high-temperature tail gas containing various concentration and its device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106000012A true CN106000012A (en) | 2016-10-12 |
| CN106000012B CN106000012B (en) | 2018-10-30 |
Family
ID=57115586
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610610661.5A Active CN106000012B (en) | 2016-07-29 | 2016-07-29 | A kind of energy-efficient recovery process of high-temperature tail gas containing various concentration and its device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106000012B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109232228A (en) * | 2018-10-19 | 2019-01-18 | 天津渤化永利化工股份有限公司 | A kind of system and method handling acetic acid plant propionic acid process tail gas |
| CN116603369A (en) * | 2023-04-28 | 2023-08-18 | 成都益志科技有限责任公司 | Absorbent capable of efficiently absorbing sulfur dioxide |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4654205A (en) * | 1986-01-15 | 1987-03-31 | C-I-L Inc. | Sulphur trioxide absorption apparatus and process |
| CN101024603A (en) * | 2007-03-29 | 2007-08-29 | 永港伟方(北京)科技有限公司 | Methanal absorbing system |
| CN103336087A (en) * | 2013-06-07 | 2013-10-02 | 中电投远达环保工程有限公司 | Testing device of desulphurization efficiency and testing method thereof |
| CN203329583U (en) * | 2013-07-04 | 2013-12-11 | 山西潞安矿业(集团)有限责任公司 | Chlorine hydride absorption device in polycrystalline silicon tail gas recovery system |
| CN105642661A (en) * | 2016-03-24 | 2016-06-08 | 浙江工商大学 | Device and process for safely treating aluminum phosphide fumigating residues |
-
2016
- 2016-07-29 CN CN201610610661.5A patent/CN106000012B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4654205A (en) * | 1986-01-15 | 1987-03-31 | C-I-L Inc. | Sulphur trioxide absorption apparatus and process |
| CN101024603A (en) * | 2007-03-29 | 2007-08-29 | 永港伟方(北京)科技有限公司 | Methanal absorbing system |
| CN103336087A (en) * | 2013-06-07 | 2013-10-02 | 中电投远达环保工程有限公司 | Testing device of desulphurization efficiency and testing method thereof |
| CN203329583U (en) * | 2013-07-04 | 2013-12-11 | 山西潞安矿业(集团)有限责任公司 | Chlorine hydride absorption device in polycrystalline silicon tail gas recovery system |
| CN105642661A (en) * | 2016-03-24 | 2016-06-08 | 浙江工商大学 | Device and process for safely treating aluminum phosphide fumigating residues |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109232228A (en) * | 2018-10-19 | 2019-01-18 | 天津渤化永利化工股份有限公司 | A kind of system and method handling acetic acid plant propionic acid process tail gas |
| CN116603369A (en) * | 2023-04-28 | 2023-08-18 | 成都益志科技有限责任公司 | Absorbent capable of efficiently absorbing sulfur dioxide |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106000012B (en) | 2018-10-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN207627955U (en) | A kind of gasification black water flash system | |
| CN104743728B (en) | A kind of energy-saving deamination method of residual coking ammonia water negative pressure deamination | |
| CN101343208B (en) | Desorption technique for methylbenzene in tail gas from benzyl chloride preparation | |
| CN103411469B (en) | A kind of cooling tower water steam and heat energy recovering method and system | |
| CN208893656U (en) | The equipment of NMP recycling heat pump distillation in a kind of production of lithium electricity | |
| CN103084043A (en) | High-efficiency spraying solvent recovery system and process thereof | |
| CN105344124A (en) | Double-rectifying-tower four-effect superior alcohol distillation method and device for preparing alcohol | |
| CN206940478U (en) | A kind of steam circulation deamination apparatus | |
| CN106000012A (en) | Efficient energy-saving recovery process and device for different concentrations of high-temperature tail gas | |
| CN108452639A (en) | The heat recovery and nmp solvent recovery method and device of a kind of lithium battery coating machine exhaust | |
| CN102584549B (en) | Process and evaporator for preparing raw material gas in methanal production | |
| CN108658095A (en) | The energy-saving reclaiming process and system that a kind of ammonium hydroxide recycling concentration is easily adjusted | |
| CN205886539U (en) | Energy -efficient recovery unit of high temperature tail gas who contains different concentration | |
| CN106187679A (en) | The recycling system and method for carbon dioxide in a kind of chlorinated hydrocabon hydrolysis tail gas | |
| CN111744328A (en) | Low-energy-consumption carbon dioxide capturing method and system for low-concentration carbon dioxide-containing tail gas | |
| CN203474477U (en) | Vapor recycling system for multi-hole ammonium nitrate production process | |
| CN204337983U (en) | The recycling treatment process system of MOCVD waste gas in a kind of LED chip production process | |
| CN203820474U (en) | Flue gas waste heat recovery and utilization device for aluminium hydroxide calcinator | |
| CN109319739A (en) | A kind of hydrogen chloride drying system and drying means | |
| CN211876787U (en) | Condenser for acetic acid concentration | |
| CN203613126U (en) | Energy-saving and efficient urea low-pressure decomposition system | |
| CN1858005A (en) | Energy saving, purifying and recovering process for urea process condensate | |
| CN209259684U (en) | A kind of hydrogen chloride drying system | |
| CN206935088U (en) | A kind of absorption integrated device of deamination | |
| CN207871852U (en) | A kind of heat recovery and nmp solvent retracting device of the exhaust of lithium battery coating machine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20161012 Assignee: Shandong Oasis Electronic Technology Co.,Ltd. Assignor: ZHEJIANG TITAN DESIGN & ENGINEERING Co.,Ltd. Contract record no.: X2023330000409 Denomination of invention: A high-efficiency energy-saving recovery process and device for high-temperature exhaust gas with different concentrations Granted publication date: 20181030 License type: Common License Record date: 20230718 |