CN106629949B - Deaerator for boiler water made from process condensate - Google Patents
Deaerator for boiler water made from process condensate Download PDFInfo
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- CN106629949B CN106629949B CN201611009680.9A CN201611009680A CN106629949B CN 106629949 B CN106629949 B CN 106629949B CN 201611009680 A CN201611009680 A CN 201611009680A CN 106629949 B CN106629949 B CN 106629949B
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- packing
- process condensate
- tower
- distributor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
- F22D1/50—Feed-water heaters, i.e. economisers or like preheaters incorporating thermal de-aeration of feed-water
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/02—Non-contaminated water, e.g. for industrial water supply
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- Engineering & Computer Science (AREA)
- Hydrology & Water Resources (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Physics & Mathematics (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
- Degasification And Air Bubble Elimination (AREA)
Abstract
The invention relates to a deaerator for boiler water preparation by process condensate, which is characterized by comprising a deaerating water tank and a deaerating tower, wherein an outlet at the top of the deaerating tower is connected with an exhaust pipe, and an outlet at the bottom of the deaerating tower is connected with the deaerating water tank; three sections of fillers arranged at intervals are sequentially filled in the deaerating tower from top to bottom; wherein a first distributor is arranged above the first section of the packing and is connected with a first condensate inlet arranged on the side wall of the deoxidizing tower; a second distributor is arranged above the second section of the packing, and an inlet of the second distributor is connected with a second condensate inlet arranged on the side wall of the deaerating tower; a steam distributor is arranged below the third section of packing, and an inlet of the steam distributor is connected with a steam inlet arranged on the side wall of the deaerating tower.
Description
Technical Field
the invention relates to the field of boiler water preparation by using acid process condensate, in particular to a deaerator for boiler water preparation by using process condensate.
Background
Traditional oxygen-eliminating device comprises water tank and oxygen-eliminating tower two parts usually, is used for desorption demineralized water dissolved oxygen and other impurity gas, because the dissolved oxygen of demineralized water is micro usually, consequently, no matter the oxygen-eliminating device of what kind of structure is adopted, the oxygen-eliminating tower only sets up one section filler usually and just can satisfy the deoxidization requirement.
At present, three main process technologies for deoxidizing boiler water by using a traditional deaerator to process condensate are provided, which are respectively as follows:
1) The process condensate is fed into a normal pressure stripping tower for stripping by self pressure to remove CO2And (3) waiting for gas with higher solubility, boosting the pressure of the process condensate at the bottom of the stripping tower by using a booster pump, and then sending the process condensate into a traditional deaerator to remove trace components such as oxygen and the like to prepare boiler water.
The disadvantages are as follows: the stripping tower and the booster pump need to be arranged independently, stripping steam needs to be arranged independently in the stripping tower, and the investment and the operating cost of the device are high.
2) The process condensate is mixed with desalted water, the process condensate is diluted by the desalted water, the concentration of dissolved gas in the process condensate is reduced, the diluted process condensate is directly sent into a traditional deaerator to remove oxygen and other dissolved gas, and the treated process condensate is directly used as boiler water.
the disadvantages are as follows: when the solubility and the dissolving amount of the gas dissolved in the process condensate are large, a large amount of desalted water needs to be consumed to dilute the process condensate, and the load and the equipment investment of the deaerator are increased.
3) The process condensate is directly sent into a traditional deaerator to remove oxygen and other dissolved gases, and the treated process condensate is directly used as boiler water.
The disadvantages are as follows: when the solubility and the dissolving amount of the gas dissolved in the process condensate are large, the traditional deaerator is difficult to completely remove the gas dissolved in the process condensate, and the quality of the prepared boiler water does not reach the standard.
Device for preparing synthesis gas by natural gas steam reforming for controlling H in reformed gas at outlet of reforming furnace2the/CO is 2.0-3.0, and a large amount of CO is supplemented into the inlet of the converter2CO in the synthesis gas at the outlet of the converter2The content of the low-pressure steam reaches up to 13 v%, the molar concentration of CO2 dissolved in process condensate obtained in the cooling and liquid separating process of the synthesis gas reaches up to 0.18%, the concentration of the dissolved oxygen in the desalted water is far greater than that of the dissolved oxygen in the desalted water, and the problems of high low-pressure steam consumption, high equipment investment, unqualified boiler water quality and the like exist in the process of preparing boiler water by adopting a traditional deaerator and the traditional process condensate.
disclosure of Invention
The invention aims to solve the technical problem of providing the deaerator for the process condensate boiler water, which has the advantages of good energy saving and consumption reduction effects, small equipment investment and good boiler water quality, aiming at the current situation of the prior art.
The technical scheme adopted by the invention for solving the technical problems is as follows: the deaerator for boiler water production by using condensate in the process is characterized by comprising a deaerating water tank and a deaerating tower, wherein an outlet at the top of the deaerating tower is connected with an exhaust pipe, and an outlet at the bottom of the deaerating tower is connected with the deaerating water tank;
Three sections of fillers arranged at intervals are sequentially filled in the deaerating tower from top to bottom; wherein a first distributor is arranged above the first section of the packing and is connected with a first condensate inlet arranged on the side wall of the deoxidizing tower; a second distributor is arranged above the second section of the packing, and an inlet of the second distributor is connected with a second condensate inlet arranged on the side wall of the deaerating tower;
A steam distributor is arranged below the third section of packing, and an inlet of the steam distributor is connected with a steam inlet arranged on the side wall of the deaerating tower.
Preferably, a first redistributor is arranged between the first section of filling material and the second redistributor for further uniformly distributing the liquid flowing downwards; and a second redistributor is arranged between the second section of packing and the third section of packing.
In order to facilitate maintenance, a first manhole, a second manhole and a third manhole can be sequentially arranged on the side wall of the oxygen removing tower from top to bottom; the first manhole is located above the first distributor, the second manhole is located between the first redistributor and the second distributor, and the third manhole is located between the second redistributor and the third section of packing.
and a first hand hole corresponding to the first section of the filler, a second hand hole corresponding to the second section of the filler and a third hand hole corresponding to the third section of the filler are formed in the side wall of the oxygen removing tower. The hand holes are arranged for discharging the packing in the tower.
The fillers in the above schemes can be specifically selected according to the composition of the treated process condensate, preferably, the fillers in the first section, the second section and the third section are all bulk fillers.
Compared with the prior art, the novel deaerator for the process condensate boiler water has the following advantages:
1. The deaerator disclosed by the invention is a novel deaerator integrating stripping and deaerating, the stripping and deaerating are simultaneously completed in one deaerator tower, gas components with high solubility and high dissolving capacity in process condensate can be effectively removed, and the deaerator is stable and reliable in deaerating effect.
2. the invention respectively sends the process condensate from the upstream to different parts of the deaerator according to different temperatures, realizes cold and hot split, scientifically and reasonably utilizes the temperature levels and energy gradients of the different process condensates, and reduces the steam consumption of the deaerator.
Drawings
Fig. 1 is a schematic plan view of an embodiment of the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1, the deaerator for boiler water making by using condensate in the process comprises a deaerating water tank 1 and a deaerating tower 2, wherein an outlet at the top of the deaerating tower 2 is connected with an exhaust pipe 3, and an outlet at the bottom of the deaerating tower 2 is connected with the deaerating water tank 1; the deoxidizing water tank is of a horizontal structure.
three sections of fillers which are arranged at intervals are sequentially filled in the deaerating tower 2 from top to bottom; a first distributor 7 is arranged above the first section of packing 12, and the first distributor 7 is connected with a first condensate inlet 4 arranged on the side wall of the deaerating tower; a second distributor 9 is arranged above the second section of the packing 13, and an inlet of the second distributor 9 is connected with a second condensate inlet 5 arranged on the side wall of the deaerating tower; a steam distributor 11 is arranged below the third section of packing 14, and an inlet of the steam distributor 11 is connected with a steam inlet 6 arranged on the side wall of the deaerating tower.
A first redistributor 8 is arranged between the first section of filling material 12 and the second redistributor 9; and a second redistributor 10 is arranged between the second section of packing 13 and the third section of packing 14.
A first manhole 15, a second manhole 16 and a third manhole 17 are sequentially arranged on the side wall of the oxygen-removing tower 2 from top to bottom; a first manhole 15 is located above the first distributor 7, a second manhole 16 is located between the first redistributor 8 and the second distributor 9, and a third manhole 17 is located between the second redistributor 10 and the third section of packing 14.
The sidewall of the oxygen removing tower 2 is provided with a first hand hole 18 corresponding to the first section of the packing 12, a second hand hole 19 corresponding to the second section of the packing 13 and a third hand hole 20 corresponding to the third section of the packing 14.
In this embodiment, the first stage packing 12, the second stage packing 13 and the third stage packing 14 are all bulk packing.
The low-temperature process condensate with the temperature of 30-60 ℃ from the upstream device enters the deaerating tower from the first condensate inlet, and after the flow is uniformly distributed by the first distributor, the low-temperature process condensate enters the first section of filler downwards.
In the first stage of packing, the low temperature process condensate is fully contacted with the low pressure steam rising from the bottom of the tower, and the CO dissolved in the process condensate2Most of other impurity gases are stripped, and the low-temperature process condensate after stripping is distributed with flow by the first redistributor and then enters the second section of packing downwards.
And the high-temperature process condensate with the temperature of 90-120 ℃ from the upstream device enters the deaerating tower from the second condensate inlet, and after the flow is uniformly distributed by the second distributor, the high-temperature process condensate and the process condensate from the first section of filler are mixed and then enter the second section of filler downwards.
The ratio of the flow rate of the low-pressure steam to the flow rate of the process condensate in the embodiment is 0.2-0.3.
In the second section of the packing, the two streams of process condensate are fully contacted with the low-pressure steam rising from the bottom of the tower, and the CO dissolved in the process condensate2And a substantial portion of the other contaminant gases are stripped away. The process condensate after steam stripping is distributed with flow by the second redistributor and then enters the third section of filler downwards.
In the third section of the filler, the two process condensate flows are fully contacted with low-pressure steam which is from a steam inlet and has the temperature of 170-200 ℃ and the pressure of 0.4-1.5 MPaG again, oxygen and other impurity gases dissolved in the process condensate are stripped, the process condensate after the oxygen and other impurity gases are removed enters an oxygen removal water tank, and the whole process of preparing boiler water from the process condensate is completed.
Claims (4)
1. The deaerator for the process condensate boiler making water is characterized by comprising a deaerating water tank (1) and a deaerating tower (2), wherein an outlet at the top of the deaerating tower (2) is connected with an exhaust pipe (3), and an outlet at the bottom of the deaerating tower (2) is connected with the deaerating water tank (1);
Three sections of fillers which are arranged at intervals are sequentially filled in the deaerating tower (2) from top to bottom; wherein a first distributor (7) is arranged above the first section of packing (12), and the first distributor (7) is connected with a first condensate inlet (4) arranged on the side wall of the oxygen removal tower; a second distributor (9) is arranged above the second section of packing (13), and an inlet of the second distributor (9) is connected with a second condensate inlet (5) arranged on the side wall of the oxygen removal tower;
A steam distributor (11) is arranged below the third section of packing (14), and an inlet of the steam distributor (11) is connected with a steam inlet (6) arranged on the side wall of the deaerating tower;
A first redistributor (8) is arranged between the first section of the packing (12) and the second redistributor (9); a second redistributor (10) is arranged between the second section of packing (13) and the third section of packing (14);
the low-temperature process condensate with the temperature of 30-60 ℃ from an upstream device enters the deaerating tower from a first condensate inlet, and after the flow is uniformly distributed by a first distributor, the low-temperature process condensate enters the first section of filler downwards;
in the first stage of packing, the low temperature process condensate is fully contacted with the low pressure steam rising from the bottom of the tower, and the CO dissolved in the process condensate2Most of other impurity gases are stripped, and the stripped low-temperature process condensate enters a second section of filler downwards after the flow is distributed by a first redistributor;
The high-temperature process condensate with the temperature of 90-120 ℃ from the upstream device enters the deaerating tower from a second condensate inlet, and after the flow is uniformly distributed by a second distributor, the high-temperature process condensate and the process condensate from the first section of filler are mixed and then enter the second section of filler downwards;
The ratio of the flow of the low-pressure steam to the flow of the process condensate is 0.2-0.3;
in the second section of the packing, the two streams of process condensate are fully contacted with the low-pressure steam rising from the bottom of the tower, and the CO dissolved in the process condensate2And most of other impurity gases are stripped; the process condensate after steam stripping is distributed with flow by a second redistributor and then enters a third section of filler downwards;
In the third section of the filler, the two process condensate flows are fully contacted with low-pressure steam with the temperature of 170-200 ℃ and the pressure of 0.4-1.5 MPaG from a steam inlet again, oxygen and other impurity gases dissolved in the process condensate are stripped, and the process condensate with the oxygen and other impurity gases removed enters the deoxygenating water tank.
2. the deaerator for process condensate boiler making water according to claim 1, characterized in that a first manhole (15), a second manhole (16) and a third manhole (17) are sequentially arranged on the side wall of the deaerator (2) from top to bottom; the first manhole (15) is located above the first distributor (7), the second manhole (16) is located between the first redistributor (8) and the second distributor (9), and the third manhole (17) is located between the second redistributor (10) and the third section of packing (14).
3. the deaerator for process condensate boiler making water according to any one of claims 1 to 2, characterized in that a first hand hole (18) corresponding to the first section of the packing (12), a second hand hole (19) corresponding to the second section of the packing (13) and a third hand hole (20) corresponding to the third section of the packing (14) are formed on the side wall of the deaerator (2).
4. The deaerator for process condensate boiler water according to claim 3, characterized in that the first stage packing (12), the second stage packing (13) and the third stage packing (14) are all bulk packing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611009680.9A CN106629949B (en) | 2016-11-16 | 2016-11-16 | Deaerator for boiler water made from process condensate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611009680.9A CN106629949B (en) | 2016-11-16 | 2016-11-16 | Deaerator for boiler water made from process condensate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106629949A CN106629949A (en) | 2017-05-10 |
| CN106629949B true CN106629949B (en) | 2019-12-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611009680.9A Active CN106629949B (en) | 2016-11-16 | 2016-11-16 | Deaerator for boiler water made from process condensate |
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| CN (1) | CN106629949B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2366858C1 (en) * | 2008-04-09 | 2009-09-10 | Закрытое акционерное общество "Энергомаш (Холдинг)" | Utilisation steam boiler plant |
| CN201537408U (en) * | 2009-09-29 | 2010-08-04 | 四川亚联高科技股份有限公司 | Purification treatment tower for producing hydrogen with natural gas |
| CN202660527U (en) * | 2012-05-25 | 2013-01-09 | 浙江中山化工集团有限公司 | Efficient boiler thermal deaerator |
| CN103209929A (en) * | 2010-11-16 | 2013-07-17 | Amt国际有限公司 | Process and apparatus for removal of oxygen from seawater |
-
2016
- 2016-11-16 CN CN201611009680.9A patent/CN106629949B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2366858C1 (en) * | 2008-04-09 | 2009-09-10 | Закрытое акционерное общество "Энергомаш (Холдинг)" | Utilisation steam boiler plant |
| CN201537408U (en) * | 2009-09-29 | 2010-08-04 | 四川亚联高科技股份有限公司 | Purification treatment tower for producing hydrogen with natural gas |
| CN103209929A (en) * | 2010-11-16 | 2013-07-17 | Amt国际有限公司 | Process and apparatus for removal of oxygen from seawater |
| CN202660527U (en) * | 2012-05-25 | 2013-01-09 | 浙江中山化工集团有限公司 | Efficient boiler thermal deaerator |
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| Publication number | Publication date |
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| CN106629949A (en) | 2017-05-10 |
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