CN110668599B - Treatment method for recycling nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater - Google Patents
Treatment method for recycling nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater Download PDFInfo
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Abstract
The invention discloses a treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater, which comprises the following steps: (1) firstly, adjusting the pH value of the ammonia nitrogen wastewater to 11.0-12.0, and performing air stripping to respectively obtain ammonia gas and residual liquid; (2) adding magnesium salt into the phosphorus-containing wastewater, introducing ammonia gas generated in the step (1) or the step (3), and then stirring for reaction; (3) standing the reaction solution obtained in the step (2); filter-pressing the precipitate to obtain struvite; and (3) combining the filtrate obtained by filter pressing and the supernatant to form a combined solution, replacing ammonia nitrogen wastewater, and repeating the step (1). According to the invention, ammonia gas prepared by an ammonia nitrogen stripping process is directly introduced into a struvite precipitation reaction system, and the complete reaction of phosphate radicals is promoted by greatly improving the proportion of nitrogen and phosphorus in the precipitation reaction, so that phosphorus in wastewater is basically removed.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater.
Background
Struvite, also known as magnesium ammonium phosphate hexahydrate (MgNH) 4 PO 4 ·6H 2 O), a white crystalline mineral having low solubility in water at normal temperature, spontaneously crystallizes to form struvite crystal precipitates when the product of the concentrations of magnesium ions, ammonium ions and phosphate ions in water exceeds the solubility product constant of magnesium ammonium phosphate. Struvite belongs to resource type substances, is an excellent slow release fertilizer, and can also be used in the fields of medicine additives, feed additives, building materials and the like. The struvite precipitation method is a good choice for removing nitrogen and phosphorus elements in the wastewater, and is ecological, environment-friendly and economic.
The application mode adopting the struvite precipitation principle comprises the following steps: aiming at ammonia nitrogen wastewater only, phosphate and magnesium salt with equivalent weight or more need to be added into the wastewater, so as to reduce the nitrogen content in the wastewater (such as patents CN102336504A and CN 103288242A); for phosphoric acid-only wastewater, an ammonium salt and a magnesium salt are required to be added to the wastewater in an amount of more than equivalent (see patent CN102690000A), and the chemical cost is high in both cases. For the wastewater containing both ammonia nitrogen and phosphorus, because the proportion of nitrogen and phosphorus in the wastewater is difficult to meet the requirement of simultaneous removal, phosphate or ammonium salt still needs to be supplemented (such as patent CN108057414A) or residual nitrogen or phosphorus is treated by a biochemical treatment mode (such as patent CN108002661A) except for adding a certain magnesium salt. In addition, aiming at high-concentration wastewater (such as phosphate ions or ammonia nitrogen ions which are more than 500mg/L), the treatment mode still has difficulty in reducing the concentration of nitrogen and phosphorus to reach the discharge standard, and the subsequent treatment is still needed, so that the competitive comprehensive benefit is difficult to obtain.
In CN108057414A, the molar ratio of ammonium ions to phosphate ions was about 20:1, and the amount of ammonium ions was large, but this was considered as a defect in this method, and therefore this method was supplemented with phosphate ions such that P: N was about 0.87 to 1.06.
Due to different treatment difficulties of various waste water, the classified export and the retreatment of various waste water on the production line of an enterprise are a development trend. The ammonia nitrogen wastewater and the phosphorus-containing wastewater are common single wastewater in industrial and agricultural production. An application method of struvite precipitation which simultaneously uses wastewater only containing ammonia and nitrogen and wastewater only containing phosphorus as a nitrogen source and a phosphorus source respectively is not available. For example, when struvite is adopted to remove ammonia nitrogen in the prior art, the added phosphorus is purchased phosphate; and when in dephosphorization, the added ammonia nitrogen is purchased ammonium chloride and the like.
The phosphorus-containing wastewater refers to phosphorus element phosphate radical (PO) 4 3- ) Monohydrogen phosphate (HPO) 4 2- ) Dihydrogen phosphate radical (H) 2 PO 4 - ) Or phosphoric acid (H) 3 PO 4 ) In the form of one or more of (a) waste water.
Disclosure of Invention
The invention aims to solve the technical problem of providing a treatment method for recovering nitrogen and phosphorus by utilizing ammonia nitrogen wastewater and phosphorus-containing wastewater.
In order to solve the technical problems, the invention provides a treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater, which comprises the following steps:
(1) firstly, adjusting the pH value of the ammonia nitrogen wastewater to 11.0-12.0, and carrying out air stripping; respectively obtaining ammonia gas and residual liquid;
(2) adding magnesium salt into the phosphorus-containing wastewater, and introducing ammonia gas generated in the step (1) or the step (3) until the molar ratio of magnesium to phosphorus in the obtained reaction system is 1.05: 1-1.15: 1, and the molar ratio of nitrogen to phosphorus is 2: 1-20: 1;
adjusting the pH value of the reaction system to 8.5-9.5, and stirring for reaction for 10-30 min;
(3) standing the reaction solution obtained in the step (2) for 2-20 hours to respectively obtain a precipitate (positioned on the lower layer) and a supernatant (positioned on the lower layer);
filter-pressing the precipitate (using a filter press) to obtain struvite (solid);
and (3) combining the filtrate obtained by filter pressing and the supernatant to form a combined solution, replacing ammonia nitrogen wastewater, and repeating the step (1).
That is, in this step, the combined filtrate and supernatant obtained by pressure filtration is also: firstly, the pH value is 11.0-12.0, and then air stripping is carried out; respectively obtaining ammonia gas and residual liquid.
In the invention, the ammonia nitrogen can be led out to the ammonia nitrogen stripping device by a pump for air stripping.
The improvement of the treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater of the invention comprises the following steps: the magnesium salt in the step (2) is magnesium sulfate or magnesium chloride.
The treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater is further improved as follows: ammonia nitrogen stripping conditions: the temperature was 30 ℃ and the gas-liquid ratio was 4000.
Namely, controlling the temperature of ammonia nitrogen wastewater/combined liquid with the pH value adjusted to 11.0-12.0 at 30 ℃, and introducing air, wherein the volume ratio of the air to the wastewater is 1: 4000.
The treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater is further improved as follows: the stirring speed in the step (2) is 100-1000 rpm.
The treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater is further improved as follows: sodium hydroxide was used to adjust the pH.
The conventional struvite precipitation idea is to adjust the molar ratio of magnesium, nitrogen and phosphorus in a reaction system to about 1:1:1 so as to remove nitrogen and phosphorus as much as possible, but in practical situations, nitrogen and phosphorus are difficult to be removed to the full extent to meet the discharge standard. The conventional ammonia nitrogen stripping concept is that stripped ammonia gas must be absorbed by adopting media such as sulfuric acid to form substances such as ammonium sulfate and the like, and then ammonia nitrogen is further utilized. The invention adopts reverse thinking, adjusts the molar ratio of nitrogen to phosphorus in the wastewater to be more than 1:1, creatively introduces ammonia gas from which ammonia nitrogen is blown out into a reaction system directly to precipitate struvite in the reaction process, and controls the introduced ammonia gas to ensure that the ammonia nitrogen in the reaction system is greatly excessive, thereby completely removing the phosphorus to reach the discharge standard.
The invention aims at treating the phosphorus-containing wastewater and recovering nitrogen and phosphorus, namely, providing ammonia gas by using ammonia nitrogen wastewater and converting phosphorus in the phosphorus-containing wastewater into struvite. The effect of wastewater treatment is reflected by the removal degree of phosphorus in phosphorus-containing wastewater, the phosphate radical content is difficult to reduce to less than 1mg/L by the conventional struvite treatment method at present, and the phosphate radical content in the combined solution obtained after treatment can be less than or equal to 0.33mg/L by the method.
In the invention, the magnesium source is added into the phosphorus-containing wastewater, ammonia gas is introduced, and then the pH is adjusted, so that the condition that magnesium phosphate is generated possibly caused by adjusting the pH first can be prevented.
The invention does not directly utilize ammonia nitrogen wastewater to carry out struvite precipitation reaction, but firstly blows out ammonia gas by an ammonia nitrogen stripping method and enters phosphorus-containing wastewater for reaction. The proportion of nitrogen and phosphorus in the reaction is realized by adjusting the amount of introduced ammonia gas.
The residual liquid obtained in the step 1) of the invention can be directly discharged if meeting the standard, otherwise, the further biochemical treatment is needed; this is common general knowledge and therefore will not be described in detail in the present invention.
The invention has the following beneficial effects:
the invention provides a new combined process of ammonia nitrogen stripping and struvite precipitation, which fully utilizes ammonia nitrogen wastewater and phosphorus-containing wastewater as a nitrogen source and a phosphorus source to carry out precipitation reaction respectively, and ammonia gas prepared by the ammonia nitrogen stripping process is directly introduced into a struvite precipitation reaction system, so that the complete reaction of phosphate radicals is promoted by greatly improving the proportion of nitrogen and phosphorus in the precipitation reaction, and the basic removal of phosphorus in wastewater is achieved; excessive ammonia nitrogen in the struvite precipitation reaction residual liquid reenters the reaction system in the form of ammonia gas again through a stripping method (as described in step 3) for recycling, so that the overall utilization rate of the ammonia nitrogen is improved; the ammonia gas can also adjust the pH value of the reaction to a certain extent, and the dosage of the alkali liquor during the reaction is reduced. The phosphorus wastewater treated by the method can ensure that the phosphorus content in the wastewater reaches the second-level standard (namely less than or equal to 1.0mg/L) of the integrated wastewater discharge standard.
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The following describes embodiments of the present invention in further detail with reference to the accompanying drawings.
FIG. 1 is a schematic view of the process flow of the treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater.
Detailed Description
The invention will be further described with reference to specific examples, but the scope of the invention is not limited thereto:
120 tons/day of ammonia nitrogen wastewater is generated in a certain factory, 2500mg/L of ammonia nitrogen (calculated by nitrogen element, the same is used hereinafter) in the wastewater, 1-2 of pH value, 100 tons/day of phosphorus-containing wastewater is generated, 4800mg/L of phosphate radical (calculated by phosphorus element, the same is used hereinafter) in the wastewater, and 1-2 of pH value.
The sodium hydroxide used hereinafter for adjusting the pH is a saturated aqueous solution of sodium hydroxide.
Embodiment 1, the treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater comprises the following steps:
the method comprises the following steps: adjusting the pH value of 1 ton of ammonia-nitrogen wastewater to 12.0, introducing the ammonia-nitrogen wastewater into an air stripping tower at a certain flow rate for air stripping, wherein the stripping temperature is 30 ℃, and the gas-liquid ratio is 4000; through detection, the ammonia nitrogen content of the stripping residual liquid is 25 mg/L; obtaining about 3960L of ammonia gas (under the standard state).
When the flow rate is 1m 3 At the time of/h, the stripping time is 1 h.
Step two: the ammonia gas (about 3960L) prepared in the first step was introduced into 0.5 ton of phosphorus-containing wastewater, and 9.8kg of magnesium sulfate (MgSO) was added thereto 4 ) At this time, the molar ratio of nitrogen to phosphorus in the reaction system is about 2.3, and the molar ratio of magnesium to phosphorus is about 1.05; then adjusting the pH value to 8.5-9.5, stirring to react for 30min, wherein white precipitates are generated, and the stirring speed is 200 rpm;
step three: pumping the reaction liquid obtained in the step two to a sedimentation tank by a pump, standing for 4 hours, and respectively obtaining supernatant and lower-layer sediment;
leading out the lower layer precipitate by a pump to a filter press for filter pressing (filter pressing is carried out until the liquid content is less than or equal to 5 percent by weight), air-drying to constant weight to obtain 18.9kg of struvite solid, combining the supernatant and the filtrate obtained after squeezing, and detecting to obtain a combined solution with the phosphate content of 0.33mg/L and the ammonia nitrogen content of 2830 mg/L; the high-concentration ammonia nitrogen wastewater is used for the next batch of ammonia nitrogen stripping treatment process.
Embodiment 2, the treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater comprises the following steps:
the method comprises the following steps: taking 4 tons of ammonia-nitrogen wastewater to adjust the pH value of the ammonia-nitrogen wastewater to 12.0, and then, adjusting the pH value to 1m 3 Introducing the flow of/h into an air stripping tower for air stripping, wherein the stripping temperature is 30 ℃, the gas-liquid ratio is 4000, and the stripping time is 4 h; through detection, the ammonia nitrogen content of the stripping residual liquid is 23 mg/L; obtain about 15850L of ammonia gas.
Step two: introducing ammonia gas (about 15850L) prepared in the first step into 1 ton of phosphorus-containing wastewater, and simultaneously adding 20.5kg of magnesium sulfate, wherein the molar ratio of nitrogen to phosphorus in the reaction system is about 4.6, and the molar ratio of magnesium to phosphorus is about 1.10; then adjusting the pH value of the wastewater to 8.5-9.5, stirring to react for 30min, wherein white precipitates are generated, and the stirring speed is 600 rpm;
step three: pumping the reaction liquid obtained in the step two to a sedimentation tank by a pump, standing for 8 hours, and respectively obtaining supernatant and lower-layer sediment;
leading out the lower-layer precipitate by a pump to a filter press for filter pressing (filter pressing is carried out until the liquid content is less than or equal to 5%), air-drying to constant weight to obtain 37.6kg of struvite solid, combining the supernatant and the filtrate obtained after squeezing, and detecting to obtain a combined solution with the phosphate content of 0.26mg/L and the ammonia nitrogen content of 7740 mg/L; the high-concentration ammonia nitrogen wastewater is used for the next batch of ammonia nitrogen stripping treatment process.
Embodiment 3, the treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus wastewater, using the combined solution obtained in embodiment 2 as a nitrogen source, comprises the following steps:
the method comprises the following steps: 1 ton of the combined solution obtained in example 2 was taken, the pH was adjusted to 12.0, and the volume was adjusted to 1m 3 Introducing the flow of/h into an air stripping tower for air stripping, wherein the stripping temperature is 30 ℃, the gas-liquid ratio is 4000, and the stripping time is 1 h; through detection, the ammonia nitrogen content of the stripping residual liquid is 32 mg/L; obtaining about 12330L of ammonia gas.
Step two: introducing the ammonia gas (about 12330L) prepared in the step one into 1 ton of phosphorus-containing wastewater, and simultaneously adding 20.5kg of magnesium sulfate, wherein the molar ratio of nitrogen to phosphorus in the reaction system is about 3.6, and the molar ratio of magnesium to phosphorus is about 1.10; then adjusting the pH value of the wastewater to 8.5-9.5, stirring to react for 20min, wherein white precipitates are generated, and the stirring speed is 400 rpm;
step three: pumping the reaction liquid in the step two to a sedimentation tank by a pump, standing for 12 hours, and respectively obtaining supernatant and lower-layer sediment;
leading out the lower layer precipitate by a pump to a filter press for filter pressing (the liquid content is less than or equal to 5 percent) and obtaining 38.8kg of struvite solid after air drying to constant weight, combining the supernatant and the filtrate obtained after squeezing, and detecting that the phosphate radical content in the combined solution is 0.55mg/L and the ammonia nitrogen content is 5540 mg/L; the high-concentration ammonia nitrogen wastewater is used for the next batch of ammonia nitrogen stripping treatment process.
Embodiment 4, the treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus wastewater, using the combined solution obtained in embodiment 3 as a nitrogen source, comprises the following steps:
the method comprises the following steps: 1 ton of the combined solution obtained in example 3 was taken, the pH was adjusted to 12.0, and the volume was adjusted to 1m 3 Introducing the flow of/h into an air stripping tower for air stripping, wherein the stripping temperature is 30 ℃, the gas-liquid ratio is 4000, and the stripping time is 1 h; through detection, the ammonia nitrogen content of the stripping residual liquid is 28 mg/L; obtaining ammonia gas of 8819L.
Step two: the ammonia gas (approx. 8819L) obtained in step one was introduced into 1 ton of phosphorus-containing wastewater while adding 17.0kg of magnesium chloride (MgCl) 2 ) At this time, the molar ratio of nitrogen to phosphorus in the reaction system is about 2.5, and the molar ratio of magnesium to phosphorus is about 1.15; adjusting the pH value of the wastewater to 8.5-9.5 by using sodium hydroxide, stirring to react to generate white precipitates, and continuously reacting for 20min at the stirring speed of 400 rpm;
step three: pumping the reaction liquid in the step two to a sedimentation tank by a pump, standing for 12 hours, and respectively obtaining supernatant and lower-layer sediment;
leading out the lower layer precipitate by a pump to a filter press for filter pressing (the liquid content is less than or equal to 5 percent) and obtaining 38.0kg of struvite solid after air drying to constant weight, combining the supernatant and the filtrate obtained after squeezing, and detecting that the phosphate radical content in the combined solution is 0.55mg/L and the ammonia nitrogen content is 3344 mg/L; the high-concentration ammonia nitrogen wastewater is used for the next batch of ammonia nitrogen stripping treatment process.
Comparative example 1, in the second step, the molar ratio of magnesium to phosphorus was changed from 1.05 to the following table 1, and the rest was the same as example 1; the comparison of the final results with example 1 is shown in table 1 below.
TABLE 1
The higher the content of magnesium ions, the more favorable the struvite precipitation reaction. When the ratio of magnesium to phosphorus is 0.9:1, the magnesium is insufficient at this time, so that much phosphorus cannot react and precipitate and remains in the wastewater, resulting in a higher phosphate content. At a magnesium to phosphorus ratio of 1:1, most of the phosphorus is already precipitated. When the ratio of magnesium to phosphorus is higher than 1.05, phosphorus can be substantially removed. However, it is obvious that the excess magnesium ions remain in the raffinate without additional effect and are not economical. Therefore, the magnesium-phosphorus ratio is set to be in the range of 1.05: 1-1.15: 1, and the method has precipitation effect and economy.
Comparative example 2, in the second step, the molar ratio of nitrogen to phosphorus in the reaction system is changed from 2.3 to the following table 2, and the rest is the same as that in example 1; the final results are shown in table 2 below in comparison with example 1.
TABLE 2
In table 2, the phosphorus removal effect is better as the nitrogen-phosphorus ratio is increased. When the nitrogen-phosphorus ratio is 1:1, most of phosphorus can be removed, but the residual phosphate radical is still high. When the nitrogen-phosphorus ratio is more than 2:1, the ammonia nitrogen is greatly excessive, and the phosphorus can be basically removed. According to the invention, the nitrogen-phosphorus ratio is set to be 2: 1-20: 1, the nitrogen consumption is unnecessarily increased continuously, and the energy consumption of ammonia nitrogen stripping is increased.
Finally, it is also noted that the above-mentioned list is only a few specific embodiments of the present invention. It is obvious that the invention is not limited to the above embodiments, but that many variations are possible. All modifications which can be derived or suggested by a person skilled in the art from the disclosure of the present invention are to be considered within the scope of the invention.
Claims (4)
1. The treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater is characterized by comprising the following steps of:
(1) firstly, adjusting the pH value of the ammonia nitrogen wastewater to 11.0-12.0, and carrying out air stripping to respectively obtain ammonia gas and residual liquid;
the ammonia nitrogen content in the ammonia nitrogen wastewater is 2500mg/L, and the pH value is 1-2;
(2) adding magnesium salt into the phosphorus-containing wastewater, and introducing ammonia gas generated in the step (1) or the step (3) until the molar ratio of magnesium to phosphorus in the obtained reaction system is 1.05: 1-1.15: 1, and the molar ratio of nitrogen to phosphorus is 2.3: 1-2.5: 1;
adjusting the pH value of the reaction system to 8.5-9.5, and stirring for reaction for 10-30 min;
the phosphate radical content of the phosphorus-containing wastewater is 4800mg/L, and the pH value is 1-2;
magnesium salt is magnesium sulfate or magnesium chloride;
(3) standing the reaction solution obtained in the step (2) for 2-20 hours to respectively obtain a precipitate and a supernatant;
filter-pressing the precipitate to obtain struvite;
and (3) combining the filtrate obtained by filter pressing and the supernatant to form a combined solution, replacing ammonia nitrogen wastewater, and repeating the step (1).
2. The treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater according to claim 1, characterized in that the ammonia nitrogen stripping conditions are as follows: the temperature was 30 ℃ and the gas-liquid ratio was 4000.
3. The treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater according to claim 1 or 2, characterized by comprising the following steps: the stirring speed in the step (2) is 100-1000 rpm.
4. The treatment method for recovering nitrogen and phosphorus by using ammonia nitrogen wastewater and phosphorus-containing wastewater according to claim 1 or 2, characterized by comprising the following steps: sodium hydroxide was used to adjust the pH.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003211186A (en) * | 2002-01-25 | 2003-07-29 | Ebara Corp | Treatment method for sewage containing nitrogen and phosphorus and treatment apparatus therefor |
| CN102674516A (en) * | 2012-05-22 | 2012-09-19 | 河海大学 | Method for circularly treating nitrogen-phosphorus wastewater |
| CN106277419A (en) * | 2015-05-29 | 2017-01-04 | 天津科技大学 | The method and apparatus that a kind of ammonia nitrogen waste water processes |
| CN106746026A (en) * | 2017-02-08 | 2017-05-31 | 佛山市新泰隆环保设备制造有限公司 | The phosphorus of phosphoric acid iron waste water and the resource recycle method of ammonia nitrogen and processing system |
| CN107792961A (en) * | 2016-09-07 | 2018-03-13 | 天津科技大学 | A kind of process equipment of ammonia nitrogen waste water processing |
-
2019
- 2019-09-19 CN CN201910883796.2A patent/CN110668599B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003211186A (en) * | 2002-01-25 | 2003-07-29 | Ebara Corp | Treatment method for sewage containing nitrogen and phosphorus and treatment apparatus therefor |
| CN102674516A (en) * | 2012-05-22 | 2012-09-19 | 河海大学 | Method for circularly treating nitrogen-phosphorus wastewater |
| CN106277419A (en) * | 2015-05-29 | 2017-01-04 | 天津科技大学 | The method and apparatus that a kind of ammonia nitrogen waste water processes |
| CN107792961A (en) * | 2016-09-07 | 2018-03-13 | 天津科技大学 | A kind of process equipment of ammonia nitrogen waste water processing |
| CN106746026A (en) * | 2017-02-08 | 2017-05-31 | 佛山市新泰隆环保设备制造有限公司 | The phosphorus of phosphoric acid iron waste water and the resource recycle method of ammonia nitrogen and processing system |
Non-Patent Citations (1)
| Title |
|---|
| 利用鸟粪石沉淀法从含磷废水中回收磷的实验研究;邹雪;《中国优秀博硕士学位论文全文数据库 工程科技Ⅰ辑》;20070630;B027-309 * |
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