CN1141287C - Integrated process and system for recovering liluted acetic acid - Google Patents
Integrated process and system for recovering liluted acetic acid Download PDFInfo
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Abstract
The present invention discloses an integrated technology method and a system for recovering diluted acetic acid, which relates to a technique for recovering acetic acid from solution containing diluted acetic acid. An organic solvent mixed by 20 to 80% of tributyl phosphate and 80 to 20% of kerosene (v/v) is used as an extraction agent. The integrated technology for recovering diluted acetic acid comprises the operation steps: extraction, vacuum distillation, solvent regeneration, oil washing, etc. Because of adopting the proper extraction agent, the energy consumption can be greatly reduced when the acetic acid is distilled and separated, and the loss of the extraction agent is reduced. Simultaneously, a solvent regeneration kettle is used for removing the impurities in the solvent so as to ensure the stable operation of the technology. An oil washing tower is used for washing the extracted wastewater, and thus, the extraction agent in the wastewater can be effectively recovered. Thus, the technology has the advantages of high recovery rate, large treating capacity, low energy consumption, little solvent loss, stable operation, etc., and is suitable for acetic acid solution whose acetic acid content is from 1 to 15%. The recovery rate of the acetic acid of the whole technology is 92%.
Description
Technical field
The present invention relates to a kind of chemical separation technology, relate in particular to a kind of integrated technology process and system that reclaims dilute acetic acid.
Background technology
Acetic acid is important light industry, industrial chemicals, is widely used in manufacturing processedes such as cellulose acetate, acetic acid alkyl esters.China produces about 300,000 tons of acetic acid per year, and still supply falls short of demand.In acetic acid production and application process, produced a large amount of acetic acid dilute solutions.From these waste water, reclaim acetic acid, have very high social benefit and economic benefit.
The method that reclaims acetic acid in the prior art from contain acetic acid containing waste water mainly contains extraction process and absorption method, electroosmose process.
Utilizing extraction process to reclaim acetic acid, is one of the most frequently used method.But current extraction process reclaims the technology of acetic acid exists following subject matter.The one, it is improper that extraction agent is selected, and caused process energy consumption big, and solvent loss is big even can not stable operation.The article that for example yellow peak, Zhang Yulin deliver " reclaims the method for acetic acid " from acid-bearing wastewater, and " petrochemical complex environment protection ", first phase pp6-9 in 1997 selects vinyl acetic monomer as extraction agent, reclaims acetic acid from the organic waste water that contains acetic acid.Though vinyl acetic monomer has bigger partition ratio (0.9-1.0), but because the boiling point (77.1) of vinyl acetic monomer is more much lower than the boiling point (118) of acetic acid, a large amount of extraction agent vinyl acetic monomers will evaporate at centrifugal station, it is very big to consume energy, and vinyl acetic monomer has bigger solubleness in water, cause extraction agent loss bigger, so vinyl acetic monomer is made extraction agent and is had more shortcoming.Also having some process using octylames is extraction agent, and Zhang Yunming (Guangxi Normal University's journal, 1994, Vol.19, No.4, pp372) all adopting tri-n-octyl amine with U.S. Pat 4353784 is that extraction agent reclaims acetic acid.In these technologies,,, brought very big difficulty for the stable operation of technology because the tri-n-octyl amine system is easy to generate emulsification when long-time operation though the extracting power of tri-n-octyl amine Dichlorodiphenyl Acetate is strong.Acetic acid is compared with other carboxylic acids, with the affinity height of water.For acetic acid, the partition ratio of most of extraction agents is all smaller, in order to reach certain extraction rate was acquired, will increase energy consumption at centrifugal station with a large amount of solvents.Should adopt boiling point to be higher than the extraction agent of acetic acid, such extraction agent needn't steam at segregation section, can cut down the consumption of energy.Based on this point, what the clear 57-197240 of Japanese Patent adopted is solvent pairs, promptly boiling point solvent and boiling point than the acetic acid low solvent higher than acetic acid is got up, and with this mixed solvent extracting acetic acid from the aqueous solution, and then the distillation extract reclaims acetic acid.In general, the solvent that the Dichlorodiphenyl Acetate partition ratio is big, its intermiscibility to water is also big.The first solvent boiling point height that this patent adopts, partition ratio is big, but also big to the intermiscibility of water, in order to overcome the shortcoming of first solvent, second solvent of employing is a lower boiling, with first solvent ratio, partition ratio is little, but little to the intermiscibility of water.This mixed solvent can suppress water to the flowing of extract, and is also highly beneficial aspect post-treatment.Though this technology has adopted mixed extractant, can effectively cut down the consumption of energy, the intermiscibility of first extraction agent and water is still bigger, has caused the extraction agent loss big.Adopt extraction process to reclaim dilute acetic acid technology at present, the loss of extraction agent directly influences the economic feasibility of technology, does not all take into full account contained extraction agent in the waste water how efficient recovery was handled in the prior art.This is because when extraction, certain extraction agent will be carried and dissolve to the dilute solution that contains acetic acid unavoidably secretly, and because the flow of waste water is very big, is generally 5-15m
3/ hr is so if do not reclaim this part extraction agent, then the loss of extraction agent is bigger.In addition, generally containing in the acetic acid containing waste water all can have some other impurity, and along with the carrying out of extraction, these impurity can accumulate in organic phase, the impurity of these accumulation can influence the character of extraction agent and the normal running of equipment, so these impurity need be separated with extraction agent
Summary of the invention
The present invention aims to provide a kind of integrated technology process and system that reclaims dilute acetic acid, by selecting suitable extraction agent and integrated technique, this technology can not only effectively be cut down the consumption of energy, the extraction agent loss is little, acetic acid rate of recovery height, and can effectively remove the impurity that in organic solvent, accumulates, guarantee the normal operation of equipment.
This integrated technique and system thereof are achieved by the following technical solution:
A kind of integrated technique system that reclaims dilute acetic acid, this system comprises extraction tower, the organic solvent recovery tower, solvent acetic acid separated device, organic solvent storage tank and corresponding connecting tube, it is characterized in that being provided with in this integrated system an organic solvent regeneration still that is used for removing the impurity that organic solvent accumulates, the regeneration still links to each other with the organic solvent storage tank by pipeline, is provided with the residue outlet bottom it; Also be provided with an oil scrubber that is used to reclaim extraction agent in this system, this oil scrubber top links to each other with pipeline with the bottom of extraction tower, its bottom is provided with the wastewater outlet pipe, is provided with the kerosene storage tank in the outside of oil scrubber, and this storage tank is communicated with the upper and lower of oil scrubber respectively by pipeline.
A kind of integrated technology process that adopts above-mentioned recovery dilute acetic acid, it is characterized in that this method is an extraction agent with 20%～80% tributyl phosphate and the composite organic solvent of 80%～20% kerosene (volume content), utilize operation stepss such as extraction, vacuum distilling, solvent reclamation, oil wash to form the integrated technique that reclaims dilute acetic acid, this processing method is carried out successively as follows:
A. the dilute solution that contains acetic acid enters the top of extraction tower by pipeline, and organic solvent enters in the tower from the bottom of extraction tower, both counter current contact mass transfers, and waste water is flowed out by the extraction tower bottom, and the organic solvent of load acetic acid is flowed out by the extraction tower top;
B. the organic solvent of load acetic acid is in pipeline enters the organic solvent recovery tower that adopts vacuum distilling, acetic acid after distillation and kerosene steam are discharged by the top exit of organic solvent recovery tower, condensation is after pipeline enters kerosene acetic acid separated device, after the phase-splitting, in pipeline all was back to the organic solvent recovery tower, got rid of by the outlet pipe of kerosene acetic acid separated device by dense acetic acid by kerosene acetic acid separated device for kerosene;
C. the organic solvent that removes behind the acetic acid enters the organic solvent storage tank by the organic solvent recovery tower through pipeline, most of organic solvent in the organic solvent storage tank enters the bottom of extraction tower through pipeline, another part then enters the solvent reclamation still through pipeline, the solvent reclamation still adopts vacuum distilling, organic solvent steam in the solvent reclamation still returns the organic solvent storage tank by pipeline after condensation, the residue that generates after distilling is discharged by the outlet conduit of solvent reclamation still bottom;
D. enter the top of oil scrubber by the effusive waste water in extraction tower bottom through pipeline, after the kerosene counter current contact that enters by the oil scrubber bottom, flow out by the oil scrubber bottom; Kerosene in the oil scrubber enters the kerosene storage tank from tower top through pipeline, kerosene in the kerosene storage tank returns the bottom of oil scrubber through pipeline, be that the interior kerosene of kerosene storage tank recycles the extraction agent that is used for reclaiming stripped waste water, the waste water that oil wash is crossed is discharged from the bottom of oil scrubber.
In above-mentioned technology, described organic solvent recovery tower and solvent reclamation still adopt vacuum distilling, and its vacuum tightness is 0.096-0.098MPa;
The present invention is applicable to that acetic acid content is the acetic acid dilute solution of 1%-15%.
The present invention is because a whole set of integrated technique that has adopted operation stepss such as extraction, vacuum distilling, solvent reclamation and oil wash to form, selected suitable mixed extractant simultaneously, its partition ratio is higher, and two components in the mixed extractant and the intermiscibility of water are all less, the extraction agent loss is little like this, and two component boiling points are all higher, can cut down the consumption of energy greatly when fractionation by distillation acetic acid, reduce the extraction agent loss.Adopt the solvent reclamation still can effectively remove impurity in the solvent simultaneously, guaranteed the steady running of technology.Adopt oil scrubber to wash stripped waste water, the extraction agent in can efficient recovery waste water.Advantages such as therefore this technology has rate of recovery height, and treatment capacity is big, and energy consumption is low, and solvent loss is little, and is stable.The rate of recovery of a whole set of technology acetic acid reaches 92%.
Description of drawings
Accompanying drawing 1 is a kind of embodiment schema of integrated technique of the present invention system.
Embodiment
Specify technological process of the present invention and concrete implementation step below in conjunction with accompanying drawing:
Integrated technique of the present invention system is mainly by extraction tower 1, organic solvent recovery tower 2, and solvent reclamation still 3 and oil scrubber 4, kerosene acetic acid separated device 5, organic solvent storage tank 6 and kerosene storage tank 7 and corresponding connecting tube are formed.Annexation between each equipment is as follows: the top of extraction tower 1 has pipeline 8 to be used to import dilute acetic acid solution, and the top of extraction tower 1 links to each other with the top of organic solvent recovery tower 2 with pipeline 9; The top of organic solvent recovery tower 2 links to each other with the top of kerosene acetic acid separated device 5 with pipeline 10, and the top of kerosene acetic acid separated device 5 links to each other with the top of organic solvent recovery tower 2 with pipeline 11; The bottom of kerosene acetic acid separated device has pipeline 12 to be used to discharge acetic acid.The bottom of organic solvent recovery tower 2 links to each other with the top of pipeline 13 and organic solvent storage tank 6.The bottom of organic solvent storage tank 6 links to each other with the bottom of extraction tower 1 with pipeline 14, and the bottom of organic solvent storage tank 6 links to each other with the top of solvent reclamation still 3 with pipeline 15.The top of solvent reclamation still 3 links to each other with the top of organic solvent storage tank 6 with pipeline 16.Solvent reclamation still 3 bottoms are provided with residue vent pipe 17.The bottom of extraction tower 1 links to each other with pipeline 18 with the top of oil scrubber 4.The bottom of kerosene storage tank 7 is linked to each other with pipeline 20 with the bottom of oil scrubber 4.The top of oil scrubber 4 is linked to each other with the top of kerosene storage tank 7 with pipeline 19.The waste water that oil scrubber 4 bottoms have pipeline 21 discharging oil washes to cross.
The concrete implementation step of this integrated technique is as follows:
Contain 1%～15% acetic acid dilute solution is entered extraction tower 1 by pipeline 8 top, with the organic solvent counter current contact mass transfer that enters by extraction tower 1 bottom, organic solvent adopts 20%6～80% tributyl phosphates and 80%～20% kerosene (volume content) to mix, and waste water is flowed out by pipeline 18 by the extraction tower bottom; The organic solvent of load acetic acid is flowed out by the extraction tower top, enters organic solvent recovery tower 2 by pipeline 9.Organic solvent recovery tower 2 adopts vacuum distilling, and vacuum tightness is 0.096-0.098MPa.Well heater and reboiler heating are adopted in the bottom of organic solvent recovery tower 2, acetic acid and kerosene steam are discharged by organic solvent recovery tower 2 top exits, condensation is after pipeline 10 enters kerosene acetic acid separated device 5, after the phase-splitting, kerosene by kerosene acetic acid separated device in pipeline 11 all is back to the organic solvent recovery tower.Dense acetic acid is got rid of by the outlet pipe 12 of kerosene acetic acid separated device 5.The organic solvent that removes behind the acetic acid enters organic solvent storage tank 6 by organic solvent recovery tower 2 through pipeline 13, and the most of organic solvent in the organic solvent storage tank 6 enters the bottom of extraction tower through pipeline 14, and another part enters solvent reclamation still 3 through pipeline 15.The solvent reclamation still adopts underpressure distillation, and vacuum tightness is 0.096-0.098Mpa.Organic solvent steam in the solvent reclamation still 3 returns organic solvent storage tank 6 by pipeline 16 after condensation.The residue of solvent reclamation still 3 bottoms is discharged by the outlet conduit 17 that is arranged on the bottom.Enter the top of oil scrubber 4 by the effusive waste water in extraction tower 1 bottom through pipeline 18, after the kerosene counter current contact that enters by oil scrubber 4 bottoms, flow out by pipeline 21 by oil scrubber 4 bottoms.Kerosene in the oil scrubber 4 enters kerosene storage tank 7 through pipeline 19, and the kerosene in the kerosene storage tank 7 enters the bottom of oil scrubber 4 through pipeline 20.The kerosene that is kerosene storage tank interior 7 can be recycled, and is used for reclaiming the extraction agent of stripped waste water.
Embodiment 1:
Flow is 5.0m
3/ hr, content is that the acetic acid dilute solution of 2.0% (mass content) enters extraction tower 1 through pipeline 8, the extraction tower height is 16.0 meters, tower diameter is 0.8 meter, organic solvent consist of 50% tributyl phosphate+50% kerosene, organic solvent enters extraction tower 1 by pipeline 14, water is in a ratio of 1: 1 mutually with organic solvent, after the two phase countercurrent flow contact, acetic acid content is 0.3% in the raffinate.The organic solvent of load acetic acid enters the middle part of organic solvent recovery tower 2 through pipeline 9 through extraction tower 1, it is 13 meters that organic solvent reclaims tower height, tower diameter is 1.2 meters, average vacuum tightness is 0.097MPa in the tower, the steam of kerosene and acetic acid enters kerosene acetic acid separated device 5 through behind the overhead condensation by pipeline 10, after the phase-splitting, dense acetic acid is discharged by the outlet pipe 12 of kerosene acetic acid separated device 5, and dense acetic acid flow is 0.22m
3/ h, containing acetic acid is 38.6%, the kerosene in the kerosene acetic acid separated device 5 is in pipeline 11 all is back to organic solvent recovery tower 2.Organic solvent acetic acid content behind the removal acetic acid is 0.3%.Organic solvent enters organic solvent storage tank 6 through pipeline 13 by organic solvent recovery tower 2.Organic solvent major part in the organic solvent storage tank 6 enters extraction tower 1 through pipeline 14, another part enters solvent reclamation still 3 by pipeline 15, the underpressure distillation of solvent reclamation still, vacuum tightness is 0.096-0.098MPa, tributyl phosphate and kerosene are all evaporated, and steam enters organic solvent storage tank 6 by pipeline 16 after condensation.Residue is discharged by the outlet pipe 17 of solvent reclamation still 3 bottoms.The waste water acetic acid content of being discharged by extraction tower 1 outlet at bottom is 0.3%, and it is 14 meters that this waste water enters tower height through pipeline 18, and tower diameter is the top of 0.6 meter oil scrubber 4, with flow be 1.0m
3The kerosene counter current contact of/h.Through the waste water behind the oil wash, its acetic acid content is 0.3%.Enter kerosene storage tank 7 by the effusive kerosene in oil scrubber 4 tops through pipeline 19, enter oil scrubber by kerosene storage tank 7 effusive kerosene through pipeline 20, TBP content can drop to very lowly in the waste water of being discharged by oil scrubber 4 bottoms, has reduced the extraction agent loss greatly.The rate of recovery of a whole set of technology acetic acid is 85%.
Embodiment 2:
Flow is 5.0m
3/ hr, content is that the acetic acid dilute solution of 10.0% (mass content) enters extraction tower 1 through pipeline 8, the extraction tower height is 18.0 meters, tower diameter is 1.2 meters, organic solvent consist of 20% tributyl phosphate+80% kerosene, organic solvent enters extraction tower 1 by pipeline 14, water is in a ratio of 3: 1 mutually with organic solvent, after the two phase countercurrent flow contact, acetic acid content is 1.0% in the raffinate.The organic solvent of load acetic acid enters the middle part of organic solvent recovery tower 2 through pipeline 9 through extraction tower 1, it is 16 meters that organic solvent reclaims tower height, tower diameter is 1.8 meters, average vacuum tightness is 0.097MPa in the tower, the steam of kerosene and acetic acid enters kerosene acetic acid separated device 5 through behind the overhead condensation by pipeline 10, after the phase-splitting, dense acetic acid is discharged by kerosene acetic acid separated device 5 outlet pipes 12, and dense acetic acid flow is 0.75m
3/ h, containing acetic acid is 60.0%, the kerosene in the kerosene acetic acid separated device 5 is in pipeline 11 all is back to organic solvent recovery tower 2.Organic solvent acetic acid content behind the removal acetic acid is 0.3%.Organic solvent enters organic solvent storage tank 6 through pipeline 13 by solvent recovery tower 2.Organic solvent parts in the organic solvent storage tank 6 pipeline 14 of flowing through enters extraction tower 1, another part enters solvent reclamation still 3 by pipeline 15, the underpressure distillation of solvent reclamation still, vacuum tightness is 0.096-0.098MPa, tributyl phosphate and kerosene are all evaporated, and steam enters organic solvent storage tank 6 by pipeline 16 after condensation.Residue is discharged by the outlet pipe 17 of solvent reclamation still 3 bottoms.The waste water acetic acid content of being discharged by extraction tower 1 outlet at bottom is 1.0%, and it is 14 meters that this waste water enters tower height through pipeline 18, and tower diameter is the top of 0.6 meter oil scrubber 4, with flow be 1.0m
3The kerosene counter current contact of/h.Through the waste water behind the oil wash, its acetic acid content is 1.0%.Enter kerosene storage tank 7 by the effusive kerosene in oil scrubber 4 tops through pipeline 19, enter oil scrubber 4 through pipeline 20 by kerosene storage tank 7 effusive kerosene.TBP content can drop to very lowly in the waste water of being discharged by oil scrubber 4 bottoms, has reduced the extraction agent loss greatly.The rate of recovery of a whole set of technology acetic acid is 90%.
Embodiment 3:
Flow is 6.0m
3/ hr, content is that the acetic acid dilute solution of 15.0% (mass content) enters extraction tower 1 through pipeline 8, the extraction tower height is 19.0 meters, tower diameter is 1.15 meters, organic solvent consist of 80% tributyl phosphate+20% kerosene, organic solvent enters extraction tower 1 by the lower inlet of extraction tower 1, water is in a ratio of 1.5: 1 mutually with organic solvent, after the two phase countercurrent flow contact, acetic acid content is 1.2% in the raffinate.The organic solvent of load acetic acid enters the middle part of organic solvent recovery tower 2 through pipeline 9 through extraction tower 1, it is 16 meters that organic solvent reclaims tower height, tower diameter is 1.5 meters, average vacuum tightness is 0.097MPa in the tower, the steam of kerosene and acetic acid enters kerosene acetic acid separated device 5 through behind the overhead condensation by pipeline 10, after the phase-splitting, dense acetic acid is discharged by the outlet pipe 12 of kerosene acetic acid separated device 5 bottoms, and dense acetic acid flow is 1.2m
3/ h, containing acetic acid is 69.0%, the kerosene in the kerosene acetic acid separated device 5 is in pipeline 11 all is back to organic solvent recovery tower 2.Organic solvent acetic acid content behind the removal acetic acid is 0.3%.Organic solvent enters organic solvent storage tank 6 through pipeline 13 by solvent recovery tower 2.Organic solvent parts in the organic solvent storage tank 6 pipeline 14 of flowing through enters extraction tower 1, another part enters solvent reclamation still 3 by pipeline 15, the underpressure distillation of solvent reclamation still, vacuum tightness is 0.096-0.098MPa, tributyl phosphate and kerosene are all evaporated, and steam enters organic solvent storage tank 6 by pipeline 16 after condensation.Residue is discharged by the outlet pipe 17 of solvent reclamation still 3 bottoms.The waste water acetic acid content of being discharged by extraction tower 1 outlet at bottom is 0.3%, and it is 14 meters that this waste water enters tower height through pipeline 18, and tower diameter is the top of 0.6 meter oil scrubber 4, with flow be 2.0m
3The kerosene counter current contact of/h.Through the waste water behind the oil wash, its acetic acid content is 1.2%.Enter kerosene storage tank 7 by the effusive kerosene in oil scrubber 4 tops through pipeline 19, enter oil scrubber 4 through pipeline 20 by kerosene storage tank 7 effusive kerosene.TBP content can drop to very lowly in the waste water of being discharged by oil scrubber 4 bottoms, has reduced the extraction agent loss greatly.The rate of recovery of a whole set of technology acetic acid is 92%.
Claims (4)
1. integrated technique system that reclaims dilute acetic acid, this system comprises extraction tower [1], organic solvent recovery tower [2], solvent acetic acid separated device [5], organic solvent storage tank [6] and corresponding connecting tube, it is characterized in that being provided with in this integrated system an organic solvent regeneration still [3] that is used for removing the impurity that organic solvent accumulates, the regeneration still links to each other with the organic solvent storage tank by pipeline, is provided with the residue outlet bottom it; Also be provided with an oil scrubber [4] that is used to reclaim extraction agent in this system, this oil scrubber top links to each other with pipeline with the bottom of extraction tower, its bottom is provided with the wastewater outlet pipe, is provided with kerosene storage tank [7] in the outside of oil scrubber, and this storage tank is communicated with the upper and lower of oil scrubber respectively by pipeline.
2. processing method that adopts the described integrated system of claim 1, it is characterized in that this method is that 20%～80% tributyl phosphate and the composite organic solvent of 80%～20% kerosene are extraction agent with volume content, utilize extraction, vacuum distilling, solvent reclamation and oil wash operation steps to form the integrated technique that reclaims dilute acetic acid, this processing method is carried out successively as follows:
A. the dilute solution that contains acetic acid enters the top of extraction tower [1] by pipeline [8], and organic solvent enters in the tower from the bottom of extraction tower, both counter current contact mass transfers, and waste water is flowed out by the extraction tower bottom, and the organic solvent of load acetic acid is flowed out by the extraction tower top;
B. the organic solvent of load acetic acid is in pipeline [9] enters the organic solvent recovery tower [2] that adopts vacuum distilling, acetic acid after distillation and kerosene steam are discharged by the top exit of organic solvent recovery tower, condensation is after pipeline [10] enters kerosene acetic acid separated device [5], after the phase-splitting, kerosene all is back in the organic solvent recovery tower through pipeline [11] by kerosene acetic acid separated device, and dense acetic acid is got rid of by the outlet pipe [12] of kerosene acetic acid separated device;
C. the organic solvent that removes behind the acetic acid enters organic solvent storage tank [6] by organic solvent recovery tower [2] through pipeline [13], most of organic solvent in the organic solvent storage tank enters the bottom of extraction tower through pipeline [14], another part then enters solvent reclamation still [3] through pipeline [15], the solvent reclamation still adopts vacuum distilling, organic solvent steam in the solvent reclamation still returns the organic solvent storage tank by pipeline [16] after condensation, the residue that generates after distilling is discharged by the outlet conduit [17] of solvent reclamation still bottom;
D. enter the top of oil scrubber [4] by the effusive waste water in extraction tower bottom through pipeline [18], after the kerosene counter current contact that enters by the oil scrubber bottom, flow out by the oil scrubber bottom; Kerosene in the oil scrubber enters kerosene storage tank [7] from tower top through pipeline [19], kerosene in the kerosene storage tank returns the bottom of oil scrubber through pipeline [20], be that the interior kerosene of kerosene storage tank recycles the extraction agent that is used for reclaiming stripped waste water, the waste water that oil wash is crossed is discharged from the bottom of oil scrubber.
3. according to the described integrated technology process of claim 2, it is characterized in that the vacuum tightness in described organic solvent recovery tower and the solvent reclamation still is 0.096-0.098Mpa.
4. according to claim 2 or 3 described integrated approaches, the acetic acid content that it is characterized in that entering the acetic acid dilute solution in the extraction tower is 1%-15%.
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