CN104696946A - Process and process system for steam exhaust liquid heat energy recovery and desalted water recovery - Google Patents
Process and process system for steam exhaust liquid heat energy recovery and desalted water recovery Download PDFInfo
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- CN104696946A CN104696946A CN201510014330.0A CN201510014330A CN104696946A CN 104696946 A CN104696946 A CN 104696946A CN 201510014330 A CN201510014330 A CN 201510014330A CN 104696946 A CN104696946 A CN 104696946A
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Abstract
The invention discloses a process and a process system for steam exhaust liquid heat energy recovery and desalted water recovery. A steam exhaust liquid is conveyed to a first-level heat exchanger and is cooled by desalted water from a mixing ion exchanger in the first-level heat exchanger, so that the temperature of the steam exhaust liquid is reduced to range from 60 DEG C to 65 DEG C; the steam exhaust liquid after cooling for the first time enters a second-level heat exchanger for cooling, and the temperature of the steam exhaust liquid is reduced to range from 45 DEG C to 50 DEG C by desalted water from an original desalted water tank in an enterprise zone in the second-level heat exchanger; the steam exhaust liquid enters a precise filter for mechanical filtration and purification, and the purified steam exhaust liquid sequentially enters a cation exchanger and the mixing iron exchanger for desalting treatment; the steam exhaust liquid becomes desalted water after desalting treatment, and the desalted water enters the first-level heat exchanger to exchange heat with the steam exhaust liquid entering the first-level heat exchanger, so that the temperature of the desalted water is raised to range from 70 DEG C to 75 DEG C. Recovered heat energy of the steam exhaust liquid is used for preheating boiler feedwater, so that other heat sources for heating the desalted water are reduced, and utilization of other fuel is reduced.
Description
Technical field
The present invention relates to new technology and the process system thereof of large chemical complex's steam lean liquor energy recovery and desalted water recovery, after being specifically related to the steam heat-exchanging of the various pressure in large chemical complex's production run process of matching pot furnace apparatus, form recovery and the recycling of heat energy and desalted water in steam lean liquor.
Background technology
Large chemical complex needs the steam using a large amount of different pressures in production run process, this just requires the necessary auxiliary construction boiler in large chemical engineering industry garden, a large amount of coal resources that burn heat to desalted water, produce steam to produce enough steam to ensure that enterprise normally runs, after the steam produced completes heat exchange in chemical plant installations, become steam lean liquor.Present enterprise enters large-scale cooling tower steam lean liquor after cooling, and use as recirculated water, the heat energy so both wasting steam lean liquor wastes desalted water.
Summary of the invention
For solving the problem, the invention provides a kind of steam lean liquor energy recovery, technique that desalted water reclaims and process system thereof, can guarantee to reclaim a large amount of heat energy and desalted water.
For achieving the above object, the present invention adopts following technical scheme:
A kind of steam lean liquor energy recovery, the process system that desalted water reclaims, steam lean liquor holding vessel is connected to the charging aperture of first-class heat exchanger by steam lean liquor pump, the discharging opening of described first-class heat exchanger is connected to accurate filter by secondary heat exchanger, described accurate filter passes through cation exchanger, mixed ion exchanger is connected to the cooling medium inlet of described first-class heat exchanger, the cooling medium outlet of described first-class heat exchanger is connected with boiler water supply desalination water tank, the cooling medium inlet of described secondary heat exchanger is connected with the original desalination water tank in garden, the original desalination water tank in garden provides cooling medium for secondary heat exchanger.Described steam lean liquor holding vessel, steam lean liquor delivery pump, first-class heat exchanger, secondary heat exchanger, accurate filter, mixed ion exchanger, cation exchanger, boiler water supply desalination water tank, the original desalination water tank in garden are by DCS control system controlling run.
Described first-class heat exchanger and secondary heat exchanger are equipped with temperature sensor.
The technique that steam lean liquor energy recovery, desalted water reclaim, concrete technology step is:
(1) temperature is the steam lean liquor of 90 ~ 95 DEG C, by Cemented filling to steam lean liquor storage tank;
(2) then use steam lean liquor transport pump to first-class heat exchanger, in first-class heat exchanger, carry out first time cooling with the desalted water from mixed ion exchanger to steam lean liquor, make steam lean liquor temperature be down to 60 DEG C-65 DEG C;
(3) the steam lean liquor after first time cooling enters secondary heat exchanger again and carries out second time cooling, in secondary heat exchanger, make steam lean liquor temperature be down to 45 DEG C-50 DEG C with the desalted water from the original desalination water tank of enterprise campus;
(4) steam lean liquor enters accurate filter and carries out mechanical filter removal of impurities, and the steam lean liquor after removal of impurities enters cation exchanger successively, mixed ion exchanger carries out desalting processing;
(5) steam lean liquor becomes desalted water through desalting processing, desalted water enters first-class heat exchanger and the steam lean liquor heat exchange entering first-class heat exchanger, make desalted water temperature increase to 70 DEG C-75 DEG C, the heat of recovered steam lean liquor carries out preheating for supplying the desalted water entering boiler water supply desalination water tank, makes heat obtain sufficient recycling;
(6) desalted water after heating up enters boiler water supply desalination water tank, is delivered in steam generator system uses by water pump.
In described step (2), steam lean liquor remains on less than 95 degrees Celsius in first-class heat exchanger inlet temperature, outlet temperature 60 DEG C-65 DEG C, below Stress control 0.6MPa, the desalted water medium temperature from mixed ion exchanger entering first-class heat exchanger is 40 DEG C, and cold and hot rate-of flow ratio is about 0.7 ~ 1.2.
In described step (3), after the desalted water in desalination water tank and the heat exchange of steam lean liquor, the cool medium in secondary heat exchanger rises to 40 DEG C by 25 DEG C.
In described step (4), the effect of cation exchanger is iron ion, sodium ion, magnesium ion, calcium ion etc. except trace in devaporation lean liquor, water outlet quality is made to be not less than following desired value: under 25 ° of C, silica < 0.1mg/L, electrical conductivity < 5s/cm.
Mixed ion exchanger is that anion and cation exchange resin is placed in same interchanger, they is mixed, so can regard as by the multiple bed of the staggered multi-stag of countless yin, yang exchanger resins.In water, the anions and canons of contained salt is by this interchanger, then by resins exchange, and obtain highly purified water.
In mixed ion exchanger, because yin, yang resin is mutually uniform, so its anions and canons exchange reaction is almost carried out simultaneously.In other words, the cation exchange of water and anion exchange repeatedly interlock and carry out.The H produced through H type clearing house
+and OH
-all can not accumulate, substantially eliminate the impact of counter ion, exchange and carry out more thorough.The water outlet quality of mixed ion exchanger meets boiler to the requirement of make-up water quality and is not less than following desired value: hardness ≈ 0 μm of ol/l,
SiO
2≤ 20 μ g/l, electrical conductivity≤0.2 μ S/cm(25 DEG C).
The invention has the beneficial effects as follows: the water resource in recovered steam lean liquor of the present invention, after simple process, supply steam generator system use, simultaneously, with the desalted water generated after the process of steam lean liquor, there is uniform temperature, and then through with the heat exchange of steam lean liquor after can direct boiler of feeding use the heat waste decreasing steam lean liquor self to save the energy, the steam lean liquor of each device in large chemical complex can be made fully to reclaim heat energy and desalted water resource by this technique.The present invention not only can reduce energy consumption, and can carry and reduce enterprise and use the consumption of a water, saving water resource and desalted water production cost thus reduce the operating cost of enterprise, increases the benefit of enterprise.
This invention flow process is simple, and automatically regulate simple, equipment investment is few.This new technology not only can the heat of recovered steam lean liquor can also make steam lean liquor become desalted water after treatment, saves the consumption of the former desalted water in garden.The heat energy of recovered steam lean liquor is for carry out preheating to boiler feedwater, reduce and use other thermal source to the heating of its desalted water, reduce the utilization of other fuel, the operating cost of the vapour system of large-size chemical garden enterprise can be reduced in the long term, increase the benefit of enterprise.
Accompanying drawing explanation
Fig. 1 is present system schematic diagram.
Wherein, the 1. original desalination water tank in steam lean liquor holding vessel, 2. steam lean liquor delivery pump, 3. first-class heat exchanger, 4. secondary heat exchanger, 5. accurate filter, 6. mixed ion exchanger, 7. cation exchanger, 8. boiler water supply desalination water tank, 9. garden.
Detailed description of the invention
Embodiment 1
As shown in Figure 1, a kind of steam lean liquor energy recovery, the process system that desalted water reclaims, steam lean liquor holding vessel 1 is connected to the charging aperture of first-class heat exchanger 3 by steam lean liquor pump 2, discharging opening the entering by secondary heat exchanger 4 of described first-class heat exchanger 3, discharging opening is connected to accurate filter 5, described accurate filter 5 is by cation exchanger 7, mixed ion exchanger 8 is connected to the cooling medium inlet of described first-class heat exchanger 3, the cooling medium outlet of described first-class heat exchanger 3 is connected with boiler water supply desalination water tank 8, the cooling medium inlet of described secondary heat exchanger 4 is connected with the original desalination water tank 9 in garden, the original desalination water tank 9 in garden provides cooling medium for secondary heat exchanger.Described first-class heat exchanger 3 and secondary heat exchanger 4 are equipped with temperature sensor.Above-mentioned each device is by DCS control system controlling run.
In Fig. 1, the direction of arrow represents the traffic direction of material, large chemical complex generation per hour 800M
3, temperature is about the steam lean liquor of 95 DEG C, steam lean liquor by Cemented filling to steam lean liquor storage tank 1, then first-class heat exchanger 3 is delivered to steam lean liquor pump 2, here once lower the temperature to it with the desalted water from mixed ion exchanger 6, steam lean liquor temperature is down to 60 DEG C, below Stress control 0.6MPa, the desalted water medium temperature from mixed ion exchanger entering first-class heat exchanger is 40 DEG C, and cold and hot rate-of flow ratio is 1.1.Steam lean liquor once after cooling enters secondary heat exchanger 4 again, steam lean liquor temperature is made to be down to 45 DEG C with the desalted water from the original desalination water tank 9 of enterprise here, cool medium in secondary heat exchanger rises to 40 DEG C by 25 DEG C, avoid the too high operational effect affecting ion-exchanger of steam lean liquor temperature, also reclaimed heat simultaneously, then enter accurate filter 5 and carry out mechanical filter removal of impurities, steam lean liquor after removal of impurities enters cation exchanger 7 successively, mixed ion exchanger 6 carries out desalting processing, from mixed ion exchanger 6 out after, desalted water enters first-class heat exchanger 3 and the steam lean liquor heat exchange entering first-class heat exchanger 3, make desalted water temperature increase to 70 DEG C, desalted water after intensification enters boiler water supply desalted water water tank 8, be delivered to steam generator system by water pump to use.Steam lean liquor finally becomes desalted water and enters boiler water supply desalination water tank 8, and then boiler of feeding uses.
The effect of cation exchanger 7 is iron ion, sodium ion, magnesium ion, calcium ion etc. except trace in devaporation lean liquor, water outlet quality is made to be not less than following desired value: under 25 ° of C, silica < 0.1mg/L, electrical conductivity < 5s/cm.
Mixed ion exchanger 6 is that anion and cation exchange resin is placed in same interchanger, they is mixed, so can regard as by the multiple bed of the staggered multi-stag of countless yin, yang exchanger resins.In water, the anions and canons of contained salt is by this interchanger, then by resins exchange, and obtain highly purified water.
In mixed ion exchanger 6, because yin, yang resin is mutually uniform, so its anions and canons exchange reaction is almost carried out simultaneously.In other words, the cation exchange of water and anion exchange repeatedly interlock and carry out.The H produced through H type clearing house
+and OH
-all can not accumulate, substantially eliminate the impact of counter ion, exchange and carry out more thorough.The water outlet quality of mixed ion exchanger 6 meets boiler to the requirement of make-up water quality and is not less than following desired value: hardness ≈ 0 μm of ol/l, SiO
2≤ 20 μ g/l, electrical conductivity≤0.2 μ S/cm(25 DEG C).
Embodiment 2
As shown in Figure 1, a kind of steam lean liquor energy recovery, the process system that desalted water reclaims, steam lean liquor holding vessel 1 is connected to the charging aperture of first-class heat exchanger 3 by steam lean liquor pump 2, discharging opening the entering by secondary heat exchanger 4 of described first-class heat exchanger 3, discharging opening is connected to accurate filter 5, described accurate filter 5 is by cation exchanger 7, mixed ion exchanger 8 is connected to the cooling medium inlet of described first-class heat exchanger 3, the cooling medium outlet of described first-class heat exchanger 3 is connected with boiler water supply desalination water tank 8, the cooling medium inlet of described secondary heat exchanger 4 is connected with the original desalination water tank 9 in garden, the original desalination water tank 9 in garden provides cooling medium for secondary heat exchanger.Described first-class heat exchanger 3 and secondary heat exchanger 4 are equipped with temperature sensor.Above-mentioned each device is by DCS control system controlling run.
In Fig. 1, the direction of arrow represents the traffic direction of material, large chemical complex generation per hour 810M
3, temperature is about the steam lean liquor of 95 DEG C, steam lean liquor by Cemented filling to steam lean liquor storage tank 1, then first-class heat exchanger 3 is delivered to steam lean liquor pump 2, here once lower the temperature to it with the desalted water from mixed ion exchanger 6, steam lean liquor temperature is down to 65 DEG C, below Stress control 0.6MPa, the desalted water medium temperature from mixed ion exchanger entering first-class heat exchanger is 40 DEG C, and cold and hot rate-of flow ratio is 0.9.Steam lean liquor once after cooling enters secondary heat exchanger 4 again, steam lean liquor temperature is made to be down to 49 DEG C with the desalted water from the original desalination water tank 9 of enterprise here, cool medium in secondary heat exchanger rises to 40 DEG C by 25 DEG C, avoid the too high operational effect affecting ion-exchanger of steam lean liquor temperature, also reclaimed heat simultaneously, then enter accurate filter 5 and carry out mechanical filter removal of impurities, steam lean liquor after removal of impurities enters cation exchanger 7 successively, mixed ion exchanger 6 carries out desalting processing, from mixed ion exchanger 6 out after, desalted water enters first-class heat exchanger 3 and the steam lean liquor heat exchange entering first-class heat exchanger 3, make desalted water temperature increase to 75 DEG C, desalted water after intensification enters boiler water supply desalination water tank 8, be delivered to steam generator system by water pump to use.Steam lean liquor finally becomes desalted water and enters boiler water supply desalination water tank 8, and then boiler of feeding uses.
The effect of cation exchanger 7 is iron ion, sodium ion, magnesium ion, calcium ion etc. except trace in devaporation lean liquor, water outlet quality is made to be not less than following desired value: under 25 ° of C, silica < 0.1mg/L, electrical conductivity < 5s/cm.
Mixed ion exchanger 6 is that anion and cation exchange resin is placed in same interchanger, they is mixed, so can regard as by the multiple bed of the staggered multi-stag of countless yin, yang exchanger resins.In water, the anions and canons of contained salt is by this interchanger, then by resins exchange, and obtain highly purified water.
In mixed ion exchanger 6, because yin, yang resin is mutually uniform, so its anions and canons exchange reaction is almost carried out simultaneously.In other words, the cation exchange of water and anion exchange repeatedly interlock and carry out.The H produced through H type clearing house
+and OH
-all can not accumulate, substantially eliminate the impact of counter ion, exchange and carry out more thorough.The water outlet quality of mixed ion exchanger 6 meets boiler to the requirement of make-up water quality and is not less than following desired value: hardness ≈ 0 μm of ol/l, SiO
2≤ 20 μ g/l, electrical conductivity≤0.2 μ S/cm(25 DEG C).
By reference to the accompanying drawings the specific embodiment of the present invention is described although above-mentioned; but not limiting the scope of the invention; one of ordinary skill in the art should be understood that; on the basis of technical scheme of the present invention, those skilled in the art do not need to pay various amendment or distortion that creative work can make still within protection scope of the present invention.
Claims (7)
1. a steam lean liquor energy recovery, the process system that desalted water reclaims, it is characterized in that: steam lean liquor holding vessel is connected to the charging aperture of first-class heat exchanger by steam lean liquor pump, the discharging opening of described first-class heat exchanger is connected to accurate filter by secondary heat exchanger, described accurate filter passes through cation exchanger, mixed ion exchanger is connected to the cooling medium inlet of described first-class heat exchanger, the cooling medium outlet of described first-class heat exchanger is connected with boiler water supply desalination water tank, the cooling medium inlet of described secondary heat exchanger is connected with the original desalination water tank in garden, above-mentioned each device is by DCS control system controlling run.
2. the process system of steam lean liquor energy recovery as claimed in claim 1, desalted water recovery, is characterized in that: described first-class heat exchanger and secondary heat exchanger are equipped with temperature sensor.
3. adopt a technique for the steam lean liquor energy recovery of process system as claimed in claim 1, desalted water recovery, it is characterized in that, concrete technology step is:
(1) temperature is the steam lean liquor of 90 ~ 95 DEG C, by Cemented filling to steam lean liquor storage tank;
(2) then use steam lean liquor transport pump to first-class heat exchanger, in first-class heat exchanger, carry out first time cooling with the desalted water from mixed ion exchanger to steam lean liquor, make steam lean liquor temperature be down to 60 DEG C-65 DEG C;
(3) the steam lean liquor after first time cooling enters secondary heat exchanger again and carries out second time cooling, in secondary heat exchanger, make steam lean liquor temperature be down to 45 DEG C-50 DEG C with the desalted water from the original desalination water tank of enterprise campus;
(4) steam lean liquor enters accurate filter and carries out mechanical filter removal of impurities, and the steam lean liquor after removal of impurities enters cation exchanger successively, mixed ion exchanger carries out desalting processing;
(5) steam lean liquor becomes desalted water through desalting processing, desalted water enters first-class heat exchanger and the steam lean liquor heat exchange entering first-class heat exchanger, make desalted water temperature increase to 70 DEG C-75 DEG C, the heat of recovered steam lean liquor carries out preheating for supplying the desalted water entering boiler water supply desalination water tank, makes heat obtain sufficient recycling;
(6) desalted water after heating up enters boiler water supply desalination water tank, is delivered in steam generator system uses by water pump.
4. the technique of steam lean liquor energy recovery as claimed in claim 3, desalted water recovery, it is characterized in that: in described step (2), steam lean liquor remains on less than 95 degrees Celsius in first-class heat exchanger inlet temperature, outlet temperature 60 DEG C-65 DEG C, below Stress control 0.6MPa, the desalted water medium temperature from mixed ion exchanger entering first-class heat exchanger is 40 DEG C, and cold and hot rate-of flow ratio is about 0.7 ~ 1.2.
5. the technique that reclaims of steam lean liquor energy recovery as claimed in claim 3, desalted water, is characterized in that: in described step (3), and after the desalted water in desalination water tank and the heat exchange of steam lean liquor, the cool medium in secondary heat exchanger rises to 40 DEG C by 25 DEG C.
6. the technique of steam lean liquor energy recovery as claimed in claim 3, desalted water recovery, it is characterized in that: in described step (4), the effect of cation exchanger is iron ion, sodium ion, magnesium ion, calcium ion except trace in devaporation lean liquor, water outlet quality is made to be not less than following desired value: under 25 ° of C, silica < 0.1mg/L, electrical conductivity < 5s/cm.
7. the technique of steam lean liquor energy recovery as claimed in claim 3, desalted water recovery, it is characterized in that: in described step (4), meet boiler to the requirement of make-up water quality through the water outlet quality of mixed ion exchanger and be not less than following desired value: under 25 ° of C, hardness ≈ 0 μm of ol/l, SiO
2≤ 20 μ g/l, electrical conductivity≤0.2 μ S/cm.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105110307A (en) * | 2015-07-29 | 2015-12-02 | 贵州开磷集团股份有限公司 | Steam condensate water heat recovery method of water desalination device combined phosphoric acid condensation device |
| CN108150998A (en) * | 2017-12-22 | 2018-06-12 | 芜湖德司节能科技有限公司 | A kind of boiler blowdown water heat energy utilization method |
| CN110469840A (en) * | 2018-05-10 | 2019-11-19 | 国家能源投资集团有限责任公司 | MTO condensate system heat-energy recovering apparatus and method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20010070659A (en) * | 2001-05-29 | 2001-07-27 | 윤장순 | Heating method using waste heat of condensate receiver tank |
| CN201485340U (en) * | 2009-07-16 | 2010-05-26 | 宝钢集团新疆八一钢铁有限公司 | Living quarter heating station condensed water processing device |
| CN101851038A (en) * | 2010-04-14 | 2010-10-06 | 广西三宝山新技术水处理有限公司 | High-temperature condensed water temperature-lowering and desalting method |
| CN103172191A (en) * | 2011-12-20 | 2013-06-26 | 上海巴安水务股份有限公司 | Whole coal chemical industry plant condensate water processing system |
| CN203668146U (en) * | 2013-12-02 | 2014-06-25 | 逸盛大化石化有限公司 | Water recycling system in PTA production process |
| CN203963911U (en) * | 2014-07-28 | 2014-11-26 | 宜昌鄂中化工有限公司 | A kind of steam condensed water waste heat recovery system |
-
2015
- 2015-01-12 CN CN201510014330.0A patent/CN104696946A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20010070659A (en) * | 2001-05-29 | 2001-07-27 | 윤장순 | Heating method using waste heat of condensate receiver tank |
| CN201485340U (en) * | 2009-07-16 | 2010-05-26 | 宝钢集团新疆八一钢铁有限公司 | Living quarter heating station condensed water processing device |
| CN101851038A (en) * | 2010-04-14 | 2010-10-06 | 广西三宝山新技术水处理有限公司 | High-temperature condensed water temperature-lowering and desalting method |
| CN103172191A (en) * | 2011-12-20 | 2013-06-26 | 上海巴安水务股份有限公司 | Whole coal chemical industry plant condensate water processing system |
| CN203668146U (en) * | 2013-12-02 | 2014-06-25 | 逸盛大化石化有限公司 | Water recycling system in PTA production process |
| CN203963911U (en) * | 2014-07-28 | 2014-11-26 | 宜昌鄂中化工有限公司 | A kind of steam condensed water waste heat recovery system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105110307A (en) * | 2015-07-29 | 2015-12-02 | 贵州开磷集团股份有限公司 | Steam condensate water heat recovery method of water desalination device combined phosphoric acid condensation device |
| CN108150998A (en) * | 2017-12-22 | 2018-06-12 | 芜湖德司节能科技有限公司 | A kind of boiler blowdown water heat energy utilization method |
| CN110469840A (en) * | 2018-05-10 | 2019-11-19 | 国家能源投资集团有限责任公司 | MTO condensate system heat-energy recovering apparatus and method |
| CN110469840B (en) * | 2018-05-10 | 2021-06-22 | 国家能源投资集团有限责任公司 | MTO condensed water system heat energy recovery device and method |
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Application publication date: 20150610 |