CN114455660A - Method for producing deaerated water by taking low-temperature heat as heat source and negative-pressure thermal deaerator system taking low-temperature heat as heat source - Google Patents
Method for producing deaerated water by taking low-temperature heat as heat source and negative-pressure thermal deaerator system taking low-temperature heat as heat source Download PDFInfo
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 227
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 claims abstract description 25
- 239000007788 liquid Substances 0.000 claims description 21
- 238000005086 pumping Methods 0.000 claims description 12
- 238000007670 refining Methods 0.000 abstract description 16
- 239000000446 fuel Substances 0.000 abstract description 6
- 239000003344 environmental pollutant Substances 0.000 abstract description 5
- 231100000719 pollutant Toxicity 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 5
- 238000001311 chemical methods and process Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 43
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 20
- 229910052760 oxygen Inorganic materials 0.000 description 20
- 239000001301 oxygen Substances 0.000 description 20
- 230000008569 process Effects 0.000 description 14
- 238000012546 transfer Methods 0.000 description 11
- 238000010438 heat treatment Methods 0.000 description 10
- 238000010612 desalination reaction Methods 0.000 description 9
- 238000012856 packing Methods 0.000 description 9
- 239000013535 sea water Substances 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000006392 deoxygenation reaction Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 230000008016 vaporization Effects 0.000 description 7
- 230000008901 benefit Effects 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 238000009834 vaporization Methods 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005194 fractionation Methods 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000003653 coastal water Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
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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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- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/046—Treatment of water, waste water, or sewage by heating by distillation or evaporation under vacuum produced by a barometric column
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (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 belongs to the technical field of chemical processes, and particularly relates to a method for producing deaerated water by taking low-temperature heat as a heat source and a negative-pressure thermal deaerator system taking the low-temperature heat as the heat source. The method provided by the invention comprises the following steps: under the negative pressure condition, after the water is subjected to heat exchange by using a low-temperature heat medium to produce steam, the steam is adopted to strip demineralized water, and the deoxidized water is obtained. The method provided by the invention uses low-temperature hot production steam as a stripping medium to prepare deoxygenated water, can effectively reduce fuel consumption, reduces the operation cost of refining enterprises, reduces pollutant emission, and is green and environment-friendly. The invention provides a way for refining and chemical enterprises to efficiently utilize low-temperature heat.
Description
Technical Field
The invention belongs to the technical field of chemical processes, and particularly relates to a method for producing deaerated water by taking low-temperature heat as a heat source and a negative-pressure thermal deaerator system taking the low-temperature heat as the heat source.
Background
The technological process of oil refining chemical industry (refining industry for short) generally includes the steps of raw material heating, reaction (or separation), product cooling and the like. To save energy consumed by heating the feedstock, the feedstock is first heated using the heat of the products or other streams of the reaction and fractionation process, and then heated in a furnace (consuming fuel) to the desired temperature for reaction or separation. Because the heat transfer needs temperature difference, a large amount of heat with low temperature level in the petroleum refining process can not be recovered through heat exchange with raw materials. This heat is called low temperature heat, and its temperature level is generally around 130 ℃. How to fully utilize low-temperature heat has important influence on reducing energy consumption, reducing pollutant discharge and improving economic benefit of refining enterprises.
At present, the low-temperature heat utilization method of the refining and chemical enterprises mainly comprises the following steps: 1. for process unit heating. The refinery is thermally coupled between units and the cryogenic heat is used in the fractionation column bottom reboiler heat source of certain light components separation units, such as: a fractionating tower of a gas fractionation plant. 2. The heat tracing agent is used for heating and refrigerating buildings or heat tracing of production systems. The low-temperature heat is exchanged with heat medium water, and the heat medium water can be used for heat tracing of an refining device or a storage and transportation system, heating of enterprises or surrounding civil buildings in winter, and refrigeration of self summer buildings of the refining and refining enterprises. The utilization mode of the low-temperature heat can utilize heat with the temperature higher than 75 ℃. The heating and cooling consumption is affected by seasons, so that the utilization mode has unstable heat demand. 3. For process unit refrigeration. The low-temperature heat and the heat medium water exchange heat and then are sent to a refrigerating device for refrigerating water. Cold water is used for process cooling that requires low operating temperatures. 4. Is used for seawater desalination. The refinery enterprises in the coastal water-deficient areas can exchange heat between low-temperature heat and heat medium water, and then convey the heat medium water to a seawater desalination device to be used as a heat source for seawater desalination. However, other processes for desalination of sea water, such as reverse osmosis, are available, and low temperature heat is not necessary. The heat utilization value of seawater desalination is not high, and the seawater desalination method is only used for seawater desalination when low-temperature heat does not have other high-value utilization modes. Moreover, inland refineries do not have conditions for desalination of seawater. And no seawater desalination device is required to be built in the water-deficient areas. 5. And generating electricity by using low-temperature heat. The low-temperature thermal power generation investment is high, and the energy utilization efficiency is very low (about 6%).
The five low-temperature heat utilization methods have limited utilization of the low-temperature heat utilization method, most of the low-temperature heat utilization methods have low utilization efficiency, and due to the fact that the low-temperature heat yield of the refining and chemical enterprises is large, a large amount of low-temperature heat cannot be reasonably utilized, and can only be discharged into the environment in the modes of circulating water cooling, air cooler cooling and the like. These processes of dumping energy also consume energy or other resources (e.g., water).
On the other hand, the refinery enterprises need to use a large amount of steam, and the steam is mainly used for driving compressors or pumps, injecting steam in the reaction or separation process, heating a reboiler heat source of a fractionating tower of a process device, heating a storage and transportation system and the like. The production of steam requires the production of deoxygenated water, and a refinery processing 1000 ten thousand tons of crude oil per year requires approximately 1200t/h of deoxygenated water. The production of deoxygenated water generally uses 1.0MPa steam as heat source. Whereas 1.0MPa steam is produced from a high temperature heat source, requiring increased fuel consumption. Ten million tons of smelting/annual refining integrated enterprises consume about 120 tons/hour of 1.0MPa steam for producing deoxygenated water. The annual cost is more than 2 billion yuan.
At present, the existing deaerator mostly adopts an atmospheric thermal deaerator, and the equipment is divided into a deaerating water tank and a deaerating head (a stripper). The deoxygenation water tank is mainly used for storing deoxygenated water of finished products, and the deoxygenation head is used for removing oxygen dissolved in the desalted water by steam stripping. The effect of the steam is to heat the demineralized water to saturation and to lower the partial pressure of oxygen in the gas phase to allow dissolved oxygen in the water to escape. The apparatus is operated at a slightly positive pressure, typically at an operating temperature of 104 ℃ and an operating pressure of 0.121MPa (absolute). Although the existing deoxygenated water preparation scheme can meet the process preparation requirements, the scheme has the main problems that the cost is to consume external steam, fuel is consumed for producing the steam, and the operation cost, the energy consumption and the pollutant (sulfur dioxide, nitrogen oxide, carbon dioxide and the like) emission of a refining enterprise are increased.
Disclosure of Invention
In view of the above, the present invention provides a method for producing deaerated water using low-temperature heat as a heat source, and a negative-pressure thermal deaerator system using low-temperature heat as a heat source. The method provided by the invention uses low-temperature hot production steam as a stripping medium to prepare deoxygenated water, can effectively reduce fuel consumption, reduces the operation cost of refining enterprises, reduces pollutant emission, and is green and environment-friendly.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a method for producing deoxygenated water by taking low-temperature heat as a heat source, which comprises the following steps of:
(1) using a low-temperature heat medium to exchange heat with water to produce steam;
(2) stripping the desalted water by using the steam to obtain deoxidized water;
the step (1) and the step (2) are both carried out under the condition of negative pressure.
Preferably, the pressure under the negative pressure condition is 7.4 to 100 kPa.
Preferably, the water is deoxygenated water.
The invention provides a negative pressure thermal deaerator system taking low-temperature heat as a heat source, which comprises:
the steam generator 1 is provided with a steam outlet, and a low-temperature heat medium heat exchange tube bundle is arranged in the steam generator 1;
the steam stripper 3 is provided with a steam inlet communicated with the steam outlet of the steam generator 1, and the stripper 3 is also provided with a desalted water inlet and a gas outlet;
the vacuum pumping device 5 is provided with a gas inlet; the gas inlet of the vacuum pumping device 5 is communicated with the gas outlet of the stripper 3.
Preferably, the steam generator 1 and the stripper 3 are combined into an integral structure.
Preferably, the steam generator 1 and the stripper 3 are of a split structure; the steam generator 1 is also provided with a water inlet;
the stripper 3 is also provided with a deoxygenated water outlet;
and a deoxygenated water outlet of the stripper 3 is communicated with a water inlet of the steam generator 1.
Preferably, the device also comprises a condenser 4, wherein the condenser 4 is provided with a gas inlet, a gas outlet and a liquid outlet;
the gas inlet of the condenser 4 is communicated with the gas outlet of the stripper 3, and the gas outlet of the condenser 4 is communicated with the gas inlet of the vacuumizing device 5.
Preferably, the device also comprises an evacuation circulating water tank 7, wherein the evacuation circulating water tank 7 is provided with a liquid inlet; the liquid inlet of the evacuated circulation water tank 7 communicates with the liquid outlet of the condenser 4.
Preferably, the system also comprises a deoxygenated water-low temperature heat exchanger 8, wherein the deoxygenated water-low temperature heat exchanger 8 is provided with a deoxygenated water inlet and a deoxygenated water outlet, and a low temperature heat medium heat exchange tube bundle is arranged in the deoxygenated water-low temperature heat exchanger 8; the steam generator 1 is also provided with a deoxygenated water outlet;
and a deoxygenated water inlet of the deoxygenated water-low-temperature heat exchanger 8 is communicated with a deoxygenated water outlet of the steam generator (1).
The invention provides a method for producing deoxygenated water by taking low-temperature heat as a heat source, which comprises the following steps of: (1) using a low-temperature heat medium to exchange heat with water to produce steam; (2) stripping the desalted water by using the steam to obtain deoxidized water; and (3) performing the step (1) and the step (2) under the condition of negative pressure. The method provided by the invention produces steam by low-temperature heat under the condition of negative pressure, and effectively reduces the vaporization temperature of water by negative pressure, thereby realizing the heat exchange of the low-temperature heat medium on the water to produce the steam serving as a stripping medium, effectively utilizing the low-temperature heat generated by refining enterprises, and reducing the energy consumption in the process of low-temperature heat rejection; meanwhile, the steam produced by low-temperature heat under the negative pressure condition strips the desalted water, the oxygen partial pressure in the steam can be further reduced under the negative pressure condition, the power for oxygen to escape from the desalted water is improved, the volume of the gas is increased under the negative pressure condition, the volume of the liquid is basically unchanged, steam stripping is carried out under the negative pressure condition, the liquid-steam volume ratio during steam stripping can be effectively reduced, the desalted water and the steam are in full contact, the liquid-steam mass transfer effect is improved, and the oxygen removal effect of steam stripping is improved.
The method for producing the deoxygenated water by taking the low-temperature heat as the heat source changes the conventional micro-positive pressure operation into the negative pressure operation, so that the vaporization temperature of the water is reduced, and the steam stripping medium of the deoxygenated water is changed from conventional external 1.0Mpa steam into low-temperature heat as the heat source to self-produce steam, so that a high-value utilization mode is found for a large amount of discarded low-temperature heat generated by refining enterprises, and a large amount of steam consumption is saved. Meanwhile, under the negative pressure operation condition, the unit consumption of steam for steam stripping is also greatly reduced, and the energy consumption is further reduced. Taking a million-ton-level refining and chemical integration enterprise as an example, the steam of 1.0Mpa consumed by the conventional preparation method of the deoxygenated water is about 120 tons/hour, 9 million tons of fuel standard coal are consumed every year, and the emission of carbon dioxide is about 27.9 million tons. The annual steam cost is about 2 billion yuan (without carbon dioxide emission reduction benefit). The annual carbon dioxide emission reduction benefit is about 1600 ten thousand yuan. By adopting the method for producing the deoxygenated water by taking the low-temperature heat as the heat source, the enterprise benefit is increased by more than 2 million yuan each year, and the pollutant emission is correspondingly reduced.
The invention provides a negative pressure thermal deaerator system taking low-temperature heat as a heat source, which comprises: the steam generator 1 is provided with a steam outlet, and a low-temperature heat medium heat exchange tube bundle is arranged in the steam generator 1; the steam stripper 3 is provided with a steam inlet communicated with the steam outlet of the steam generator 1, and the stripper 3 is also provided with a desalted water inlet and a gas outlet; a vacuum-pumping device 5 provided with a gas inlet; the gas inlet of the vacuum pumping device 5 is communicated with the gas outlet of the stripper 3. The negative-pressure thermal deaerator system taking low-temperature heat as a heat source provided by the invention is characterized in that a steam generator 1, a stripper 3 and a vacuumizing device 5 are communicated, a negative-pressure operation condition is provided for the steam generator 1 and the stripper 3 through the vacuumizing device 5, low-temperature heat is utilized to produce steam through a low-temperature heat medium heat exchange tube bundle positioned in the steam generator 1, the steam is contacted with demineralized water in the stripper 3 after entering the stripper for mass transfer, and deaerated water is obtained and then flows out of the system through a deaerated water outlet of the steam generator 1.
Drawings
Fig. 1 is a schematic view of a negative-pressure thermal deoxygenation system using low-temperature heat as a heat source according to embodiment 1 of the present invention;
FIG. 2 is a schematic view of a negative pressure thermal oxygen removal system using low temperature heat as a heat source according to example 2 of the present invention;
FIG. 3 is a schematic diagram of a prior art deaerator system;
the system comprises a steam generator 1, a deaerating water pump 2, a stripper 3, a condenser 4, a vacuumizing device 5, a water circulating pump 6, a circulating water tank 7, a deaerating water-low-temperature heat exchanger 8, a demineralized water pipe Q1, a low-temperature heat medium inlet pipe Q2 of the steam generator, a low-temperature heat medium outlet pipe Q3 of the steam generator, a deaerating water outlet pipe Q4, a low-temperature heat medium inlet pipe Q5 of the deaerating water-low-temperature heat exchanger, and a low-temperature heat medium outlet pipe Q6 of the deaerating water-low-temperature heat exchanger.
Detailed Description
The invention provides a method for producing deoxygenated water by taking low-temperature heat as a heat source, which comprises the following steps of:
(1) using a low-temperature heat medium to exchange heat with water to produce steam;
(2) stripping the desalted water by using the steam to obtain deoxidized water;
and (3) performing the step (1) and the step (2) under the condition of negative pressure.
The invention uses low-temperature heat medium to exchange heat with water to produce steam under the condition of negative pressure.
In the invention, the pressure of the negative pressure condition is preferably 7.4-100 kPa during the steam production.
In the present invention, the water is preferably oxygen-removed water.
In the present invention, the heat exchange is preferably performed in a steam generator.
After steam is obtained, the steam is adopted to strip demineralized water under the condition of negative pressure, and the deoxidized water is obtained.
In the invention, the pressure of the negative pressure condition is preferably 7.4-100 kPa during the stripping of the desalted water.
In the present invention, it is preferable that the steam and the desalted water are contacted in countercurrent at the time of the stripping.
In the invention, the steam stripping is preferably carried out in a steam stripper, the desalted water flows from top to bottom in the steam stripper, the steam flows from bottom to top in the steam stripper, the desalted water and the steam are in reverse contact for mass transfer, and dissolved oxygen in the desalted water escapes into the steam to obtain deoxygenated water.
In the present invention, the deoxygenated water is preferably pressurized by a deoxygenated water pump and then increased in temperature by a deoxygenated water-low temperature heat exchanger.
The invention provides a negative pressure thermal deaerator system taking low-temperature heat as a heat source, which comprises:
the steam generator 1 is provided with a deaerated water outlet, and a low-temperature heat medium heat exchange tube bundle is arranged in the steam generator 1;
the steam stripper 3 is provided with a steam inlet and a steam outlet, and the steam inlet is communicated with the steam outlet of the steam generator 1, and the steam stripper 3 is also provided with a desalted water inlet and a gas outlet;
a vacuum-pumping device 5 provided with a gas inlet; the gas inlet of the vacuum pumping device 5 is communicated with the gas outlet of the stripper 3.
The negative pressure thermal deaerator system using low-temperature heat as a heat source preferably further comprises a deaerated water-low-temperature heat exchanger 8, and in the invention, the deaerated water-low-temperature heat exchanger 8 preferably heats deaerated water entering the deaerated water-low-temperature heat exchanger 8.
As a specific embodiment of the present invention, the deoxygenated water-low temperature heat exchanger 8 is provided with a deoxygenated water inlet and a deoxygenated water outlet, and a low temperature heat medium heat exchange tube bundle is arranged in the deoxygenated water-low temperature heat exchanger 8; and a deoxygenated water inlet of the deoxygenated water-low temperature heat exchanger 8 is communicated with a deoxygenated water outlet of the steam generator 1.
As a specific embodiment of the present invention, one end of the low-temperature heat medium heat exchange tube bundle in the deoxygenated water-low-temperature heat exchanger 8 is communicated with the low-temperature heat medium inlet pipe Q5; the other end of the low-temperature heat medium heat exchange tube bundle is communicated with a low-temperature heat medium discharge pipeline Q6.
As an embodiment of the present invention, the low-temperature heat medium inlet pipe Q5 is communicated with one end of the low-temperature heat medium heat exchange tube bundle through the bottom surface of the deoxygenated water-low-temperature heat exchanger, and the low-temperature heat medium outlet pipe Q6 is communicated with the other end of the low-temperature heat medium heat exchange tube bundle through the top surface of the deoxygenated water-low-temperature heat exchanger.
As an embodiment of the present invention, the deoxygenated water outlet of the deoxygenated water-low temperature heat exchanger 8 is communicated with a deoxygenated water discharge pipe Q4.
The negative-pressure thermal deaerator system using low-temperature heat as a heat source preferably further comprises a deaerating water pump 2, and in the invention, the deaerating water pump 2 is used for pressurizing deaerating water entering the deaerating water pump 2.
As a specific embodiment of the present invention, the deoxygenation water pump 2 is provided with a water inlet and a water outlet, the water inlet of the deoxygenation water pump 2 is communicated with the deoxygenated water outlet of the steam generator 1, and the water outlet of the deoxygenation water pump 2 is communicated with the deoxygenated water inlet of the deoxygenated water-low temperature heat exchanger 8.
The invention provides a negative-pressure thermal deaerator system taking low-temperature heat as a heat source, which comprises a steam generator 1, wherein the steam generator 1 is provided with a steam outlet, and a low-temperature heat medium heat exchange tube bundle is arranged in the steam generator 1.
As one specific embodiment of the invention, one end of the low-temperature heat medium heat exchange tube bundle is communicated with a low-temperature heat medium inlet pipe Q2; the other end of the low-temperature heat medium heat exchange tube bundle is communicated with a low-temperature heat medium discharge pipeline Q3.
As an embodiment of the present invention, the low temperature heat medium inlet pipe Q2 and the low temperature heat medium outlet pipe Q3 are located on the same side of the steam generator 1.
In the invention, the low-temperature heat medium heat exchange tube bundle is used for introducing a low-temperature heat medium.
In the invention, the deoxygenated water in the steam generator 1 is contacted with the low-temperature heat medium heat exchange tube, and heat exchange is carried out on the surface of the low-temperature heat medium heat exchange tube to obtain steam.
As an embodiment of the invention, the steam generator 1 is further provided with a water inlet.
As a specific embodiment of the present invention, the steam generator 1 is further provided with an oxygen-removed water outlet.
As an embodiment of the present invention, the steam generator 1 has a horizontal type structure.
As an embodiment of the present invention, the oxygen-removed water outlet of the steam generator 1 is located on the bottom surface of the steam generator 1.
As an embodiment of the present invention, the deaerated water inlet of the steam generator 1 is located on the top surface of the steam generator 1.
As an embodiment of the invention, the steam outlet of the steam generator 1 is located on the top surface of the steam generator 1.
The negative-pressure thermal deaerator system taking low-temperature heat as a heat source comprises a stripper 3, wherein a steam inlet is communicated with a steam outlet of a steam generator (1), and the stripper 3 is also provided with a desalted water inlet and a gas outlet.
As an embodiment of the invention, the stripper 3 is of a vertical configuration.
As an embodiment of the present invention, a section of packing layer is disposed in the stripper 3.
The present invention has no particular requirement on the specific type of the filler.
In the present invention, the inlet for demineralized water of the stripper 3 is located on the side wall of the stripper 3 close to the top surface.
As a specific embodiment of the present invention, the height of the desalted water inlet of the stripper 3 is greater than the height of the packing layer.
As a particular embodiment of the invention, the demineralized water inlet of the stripper 3 communicates with a demineralized water conduit Q1.
As a specific embodiment of the present invention, the demineralized water pipe Q1 extends into the stripper 3 from the demineralized water inlet of the stripper 3, and the part of the demineralized water pipe Q1 extending into the interior of the stripper 3 is provided with a plurality of spray heads or other type of distributors, which can uniformly spray the demineralized water in the demineralized water pipe Q1 into the packing in the stripper 3.
As a specific embodiment of the present invention, the gas outlet of the stripper 3 is located on the top surface of the stripper 3.
In the present invention, the stripper 3 is preferably further provided with an oxygen-depleted water outlet and a steam inlet.
As a specific embodiment of the present invention, the demineralized water outlet of the stripper 3 is located on the bottom surface of the stripper 3.
As a particular embodiment of the invention, the steam inlet of the stripper 3 is located on the side wall of the stripper 3 close to the bottom surface.
In the present invention, the steam generator 1 and the stripper 3 are preferably combined into an integral structure.
In the present invention, when the steam generator 1 and the stripper 3 are preferably combined into an integral structure, the number of the strippers 3 is preferably 1 to 5.
As a specific embodiment of the present invention, the steam generator 1 and the 1 stripper 3 are combined into an integrated structure.
In the present invention, the steam generator 1 and the stripper 3 are preferably of a split structure.
As a specific embodiment of the present invention, when the steam generator 1 and the stripper 3 are a split structure, the oxygen-removed water outlet of the stripper 3 is communicated with the water inlet of the steam generator 1.
The negative pressure thermal deaerator system using low-temperature heat as a heat source provided by the invention preferably further comprises a condenser 4, and in the invention, the condenser 4 is used for condensing and separating gas discharged from the stripper 3.
As a specific embodiment of the present invention, the condenser 4 is provided with a gas inlet, a gas outlet and a liquid outlet, the gas inlet of the condenser 4 is communicated with the gas outlet of the stripper 3, and the gas outlet of the condenser 4 is communicated with the gas inlet of the vacuum-pumping device 5.
As an embodiment of the present invention, the liquid outlet of the condenser 4 communicates with the liquid inlet of the evacuated circulation water tank 7.
The negative-pressure thermal deaerator system using low-temperature heat as a heat source preferably comprises a vacuumizing device 5, and in the invention, the vacuumizing device 5 is preferably used for vacuumizing the stripper 3 and the steam generator 1.
As a specific embodiment of the present invention, the vacuum-pumping device is provided with a gas inlet; and a gas inlet of the vacuumizing device 5 is communicated with a gas outlet of the condenser 4.
As an embodiment of the present invention, the evacuation device 5 is provided with a drain port, and the drain port of the evacuation device is communicated with the liquid inlet of the evacuated circulation water tank 7.
As an embodiment of the present invention, the vacuum pumping device 5 is a hydraulic vacuum pump, a water ring vacuum pump or a steam vacuum pump.
As a specific embodiment of the invention, the vacuum-pumping device is one-stage or two-stage.
The negative pressure thermal deaerator system using low temperature heat as a heat source provided by the present invention preferably further comprises an evacuated circulation water tank 7, and in the present invention, the evacuated circulation water tank 7 is used for storing condensed water generated by the condenser 4 and the vacuum extractor 5.
As a specific embodiment of the present invention, the evacuated circulation water tank 7 is provided with a liquid inlet; the liquid inlet of the evacuated circulation water tank 7 communicates with the liquid outlet of the condenser 4.
As an embodiment of the invention, the evacuated circulation water tank 7 is provided with a liquid outlet.
As an embodiment of the present invention, the evacuation circulation water tank 7 is provided with a gas discharge port.
The negative pressure thermal deaerator system using low-temperature heat as a heat source provided by the invention preferably further comprises a water circulating pump 6, and in the invention, the water circulating pump 6 is used for pressurizing the condensed water in the pumped-out circulating water tank 7 and then circularly conveying the pressurized condensed water to the vacuumizing device 5.
The negative pressure thermal deaerator system using the low-temperature heat as the heat source preferably uses the low-temperature heat as the heat source to produce deaerated water. The specific production method for producing the deoxygenated water by adopting the negative-pressure thermal deoxygenator system with the low-temperature heat as the heat source in the technical scheme comprises the following steps: the desalted water enters the stripper 3 through a desalted water pipeline Q1 and then is sprayed to the upper part of the packing, and the steam rising from the lower part of the water on the surface of the packing is subjected to mass transfer and heat transfer to obtain the deoxidized water. The deoxygenated water falling by gravity from the stripper 3 enters the steam generator 1, exchanges heat with the low-temperature heat medium in the low-temperature heat medium heat exchange tube bundle in the steam generator 1 on the surface of the tube bundle, the water is heated and partially vaporized, and the vaporized steam rises to enter the stripper 3 as a stripping medium. The deaerated water is pumped out from a deaerated water outlet of the steam generator 1, enters the deaerated water pump 2, is pressurized, enters the deaerated water-low temperature heat exchanger 8, and is heated by a low-temperature heat medium in a low-temperature heat medium pipe bundle in the deaerated water-low temperature heat exchanger 8. The gas (including water vapor and oxygen) discharged from the stripper 3 enters a condenser, the steam is condensed and then enters an evacuation circulating water tank 7, the non-condensable gas enters a vacuumizing device 5, the water discharged by the vacuumizing device 5 enters the evacuation circulating water tank 7, and the evacuation circulating water tank 7 separates the oxygen and the water. The water pumped out from the liquid outlet of the pumped-out circulating water tank 7 enters the vacuumizing device 5 after being pressurized by the water circulating pump 6.
In the present invention, in the steam generator 1, the process of vaporizing the deaerated water on the heat exchange tubes can further enhance the deaerating effect.
In the present invention, increasing the steam flow in the top vent gas of the stripper 3 improves the oxygen removal effect. Because the condenser is arranged, the water vapor in the gas discharged from the top of the stripper 3 is condensed, and the flow of the water vapor can be controlled according to the oxygen removal requirement.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
According to the schematic diagram of the negative-pressure thermal deoxygenation system with low-temperature heat as a heat source shown in fig. 1, when the yield of deoxygenated water is small, a steam generator 1 and 1 stripper 3 are combined into an integrated structure, a vacuumizing device 5 is a primary hydraulic evacuator, the side surface of the stripper 3 is connected with a desalted water pipeline Q1, a gas outlet on the top surface of the stripper 3 is communicated with an overhead condenser 4, and the overhead condenser 4 is communicated with the hydraulic evacuator; and a deoxygenated water outlet of the steam generator 1 is connected with a deoxygenated water pump 2, the deoxygenated water pump 2 is communicated with a deoxygenated water-low temperature heat exchanger 8, and deoxygenated water after pressurization heat exchange is conveyed to a downstream steam generating device. One end of a low-temperature heat medium heat exchange tube bundle in the steam generator 1 is communicated with a low-temperature heat medium inlet pipeline Q2; the other end of the low-temperature heat medium heat exchange tube bundle is communicated with a low-temperature heat medium discharge pipeline Q3, the low-temperature heat medium inlet pipeline Q2 and the low-temperature heat medium discharge pipeline Q3 are positioned on the same side of the steam generator 1, the low-temperature heat medium inlet pipeline Q2 is arranged on the lower portion of the side face of the steam generator, the low-temperature heat medium discharge pipeline Q3 is arranged on the upper portion of the side face of the steam generator, regulating valves are mounted on the demineralized water pipeline Q1 and the low-temperature heat medium discharge pipeline Q3, and the regulating valves are connected with an automatic control system and used for automatically controlling the liquid level of the steam generator.
The process flow for producing the deoxygenated water by using the negative-pressure thermal deoxygenation system taking low-temperature heat as a heat source shown in fig. 1 is as follows: the desalted water enters the stripper 3 through a desalted water pipeline Q1 and then is sprayed to the upper part of the packing, and the steam rising from the lower part of the water on the surface of the packing is subjected to mass transfer and heat transfer to obtain the deoxidized water. The deoxidized water falling by gravity from the stripper 3 enters the steam generator 1, exchanges heat with the low-temperature heat medium in the low-temperature heat medium tube bundle in the steam generator 1 on the surface of the tube bundle, the water is heated and partially vaporized, and the vaporized steam rises to enter the stripper 3 as the stripping medium. The deaerated water is pumped out from a deaerated water outlet of the steam generator 1, enters the deaerated water pump 2, is pressurized, enters the deaerated water-low temperature heat exchanger 8, and is heated by a low-temperature heat medium in a low-temperature heat medium pipe bundle in the deaerated water-low temperature heat exchanger 8. The gas (including water vapor and oxygen) discharged from the stripper 3 enters a condenser, the steam is condensed and then enters an evacuation circulating water tank 7, the non-condensable gas enters a vacuumizing device 5, the water discharged by the vacuumizing device 5 enters the evacuation circulating water tank 7, and the evacuation circulating water tank 7 separates the oxygen and the water. The water pumped out from the liquid outlet of the pumped-out circulating water tank 7 enters the vacuumizing device 5 after being pressurized by the water circulating pump 6.
Example 2
The schematic diagram of the negative pressure thermal oxygen removal system using low temperature heat as a heat source shown in fig. 2 is substantially the same as that of example 1, except that: when the equipment size is great, its arrangement receives the installation space restriction, and wherein steam generator 1 and 1 stripper 3 combination are split type structure, the deoxidization water export of stripper 3 with the deoxidization water entry intercommunication of steam generator 1, the steam inlet of stripper 3 with the steam outlet intercommunication of steam generator 1.
In the present invention, the steam generator functions as: 1. low-temperature heat generated steam is used as a stripping medium; 2. the process of vaporizing water on the heat exchange tube further enhances the oxygen removing effect.
In the present invention, the operating pressure of the steam generator 1 determines the vaporization temperature of water, and the saturated vapor pressure of water at each temperature is as shown in the following table 1:
TABLE 1 saturated vapor pressure of water at various temperatures
| Temperature of | Saturated vapor pressure of water kpa (mmHg) (absolute pressure) |
| 50 | 12.33(92.51) |
| 60 | 19.91(149.4) |
| 70 | 31.16(233.7) |
| 80 | 47.34(355.1) |
In the present invention, the lower the operating pressure of the steam generator 1, the lower the vaporization temperature of the water, and the lower the heat source temperature level that can be utilized and the more heat recovered, for the same heat transfer temperature difference. If the vaporization temperature of water is set to 60 c (the operating pressure is determined to be 19.91kpa) and the cold end heat transfer temperature difference is set to 10 c, heat of the hot material above 70 c can be utilized. When the temperature of the heat source is 130 ℃, the heat with the temperature difference of 60 ℃ can be recovered. In the present invention, the specific operating pressure is optimally determined depending on the cold post-temperature of the heat source, the operating parameter requirements of the stripper.
The present invention has the following advantages by changing the operating pressure of the stripper 3 and the steam generator 1 from the conventional micro-positive pressure to the negative pressure:
1. on the basis of reducing the oxygen partial pressure by the steam stripping steam, the oxygen partial pressure of the gas phase is further reduced, and the power for oxygen to escape from water is increased;
2. the saturation temperature of the water is reduced, the steam consumption for heating the water to a saturated state is reduced, and the filling height of the heating section is reduced;
3. conditions are created for the steam generator 1 to use a low-temperature heat source;
4. the volume of gas increases at negative pressure, while the volume of liquid is essentially constant. Therefore, the negative pressure operation can reduce the liquid-vapor volume ratio on the packing layer, so that water and vapor can be more fully contacted on the packing layer, thereby improving the heat and mass transfer effects.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (9)
1. A method for producing deoxygenated water by taking low-temperature heat as a heat source comprises the following steps:
(1) using a low-temperature heat medium to exchange heat with water to produce steam;
(2) stripping the desalted water by using the steam to obtain deoxidized water;
and (3) performing the step (1) and the step (2) under the condition of negative pressure.
2. The method according to claim 1, wherein the pressure of the negative pressure condition is 7.4 to 100 kPa.
3. The method of claim 1, wherein the water is deoxygenated water.
4. A negative pressure thermal deaerator system using low temperature heat as a heat source, comprising:
the steam generator (1), the steam generator (1) is provided with a steam outlet, and a low-temperature heat medium heat exchange tube bundle is arranged in the steam generator (1);
the steam inlet of the stripper (3) is communicated with the steam outlet of the steam generator (1), and the stripper (3) is also provided with a desalted water inlet and a gas outlet;
the vacuum pumping equipment (5), wherein the vacuum pumping equipment (5) is provided with a gas inlet; the gas inlet of the vacuumizing device (5) is communicated with the gas outlet of the stripper (3).
5. The negative-pressure thermal deaerator system using low-temperature heat as a heat source according to claim 4, characterized in that the steam generator (1) and the stripper (3) are combined into an integral structure.
6. The negative-pressure thermal deaerator system taking low-temperature heat as a heat source as claimed in claim 4, characterized in that the steam generator (1) and the stripper (3) are of a split structure; the steam generator (1) is also provided with a water inlet;
the stripper (3) is also provided with a deoxygenated water outlet;
and a deoxygenated water outlet of the stripper (3) is communicated with a water inlet of the steam generator (1).
7. The negative-pressure thermal deaerator system using low-temperature heat as a heat source according to claims 4-6, characterized by further comprising a condenser (4), wherein the condenser (4) is provided with a gas inlet, a gas outlet and a liquid outlet;
and a gas inlet of the condenser (4) is communicated with a gas outlet of the stripper (3), and a gas outlet of the condenser (4) is communicated with a gas inlet of the vacuumizing device (5).
8. The negative-pressure thermal deaerator system using low-temperature heat as a heat source according to claim 7, further comprising an evacuated circulation water tank (7), wherein the evacuated circulation water tank (7) is provided with a liquid inlet; the liquid inlet of the evacuation circulating water tank (7) is communicated with the liquid outlet of the condenser (4).
9. The negative-pressure thermal deaerator system using low-temperature heat as a heat source according to any one of claims 4 to 6, further comprising a deaerated water-low-temperature heat exchanger (8), wherein the deaerated water-low-temperature heat exchanger (8) is provided with a deaerated water inlet and a deaerated water outlet, and a low-temperature heat medium heat exchange tube bundle is arranged in the deaerated water-low-temperature heat exchanger (8); the steam generator (1) is also provided with a deoxygenated water outlet;
and a deoxygenated water inlet of the deoxygenated water-low-temperature heat exchanger (8) is communicated with a deoxygenated water outlet of the steam generator (1).
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| CN202210131315.4A CN114455660A (en) | 2022-02-14 | 2022-02-14 | Method for producing deaerated water by taking low-temperature heat as heat source and negative-pressure thermal deaerator system taking low-temperature heat as heat source |
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| CN202210131315.4A CN114455660A (en) | 2022-02-14 | 2022-02-14 | Method for producing deaerated water by taking low-temperature heat as heat source and negative-pressure thermal deaerator system taking low-temperature heat as heat source |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5870877A (en) * | 1981-10-21 | 1983-04-27 | Ishikawajima Harima Heavy Ind Co Ltd | Deaerator for desalinator |
| JPS58133881A (en) * | 1982-02-02 | 1983-08-09 | Ishikawajima Harima Heavy Ind Co Ltd | Deaerator for desalting installation |
| CN202105453U (en) * | 2011-03-08 | 2012-01-11 | 宫强 | Recycling device for discharged vapor of deaerator |
| CN104445483A (en) * | 2014-11-11 | 2015-03-25 | 常州市品鑫除尘设备有限公司 | Vacuum deaerator structure |
| US20150166371A1 (en) * | 2012-07-31 | 2015-06-18 | International Business Machines Corporation | Desalination system and method for desalination |
| CN204910833U (en) * | 2015-04-16 | 2015-12-30 | 新能凤凰（滕州）能源有限公司 | Gasification oxygen -eliminating device steam heat reclaim unit |
| CN113526600A (en) * | 2021-06-17 | 2021-10-22 | 中国恩菲工程技术有限公司 | Desalting and deoxidizing equipment and desalting and deoxidizing method |
-
2022
- 2022-02-14 CN CN202210131315.4A patent/CN114455660A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5870877A (en) * | 1981-10-21 | 1983-04-27 | Ishikawajima Harima Heavy Ind Co Ltd | Deaerator for desalinator |
| JPS58133881A (en) * | 1982-02-02 | 1983-08-09 | Ishikawajima Harima Heavy Ind Co Ltd | Deaerator for desalting installation |
| CN202105453U (en) * | 2011-03-08 | 2012-01-11 | 宫强 | Recycling device for discharged vapor of deaerator |
| US20150166371A1 (en) * | 2012-07-31 | 2015-06-18 | International Business Machines Corporation | Desalination system and method for desalination |
| CN104445483A (en) * | 2014-11-11 | 2015-03-25 | 常州市品鑫除尘设备有限公司 | Vacuum deaerator structure |
| CN204910833U (en) * | 2015-04-16 | 2015-12-30 | 新能凤凰（滕州）能源有限公司 | Gasification oxygen -eliminating device steam heat reclaim unit |
| CN113526600A (en) * | 2021-06-17 | 2021-10-22 | 中国恩菲工程技术有限公司 | Desalting and deoxidizing equipment and desalting and deoxidizing method |
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