CN107388847A - Heat reclaim unit and technique in flue gas desulfurization and denitration technique - Google Patents
Heat reclaim unit and technique in flue gas desulfurization and denitration technique Download PDFInfo
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- CN107388847A CN107388847A CN201710565493.7A CN201710565493A CN107388847A CN 107388847 A CN107388847 A CN 107388847A CN 201710565493 A CN201710565493 A CN 201710565493A CN 107388847 A CN107388847 A CN 107388847A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C1/00—Direct-contact trickle coolers, e.g. cooling towers
- F28C1/02—Direct-contact trickle coolers, e.g. cooling towers with counter-current only
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C1/00—Direct-contact trickle coolers, e.g. cooling towers
- F28C1/003—Direct-contact trickle coolers, e.g. cooling towers comprising outlet ducts for exhaust gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C1/00—Direct-contact trickle coolers, e.g. cooling towers
- F28C1/08—Arrangements for recovering heat from exhaust steam
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C1/00—Direct-contact trickle coolers, e.g. cooling towers
- F28C1/14—Direct-contact trickle coolers, e.g. cooling towers comprising also a non-direct contact heat exchange
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F25/00—Component parts of trickle coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F25/00—Component parts of trickle coolers
- F28F2025/005—Liquid collection; Liquid treatment; Liquid recirculation; Addition of make-up liquid
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention relates to the heat reclaim unit in a kind of flue gas desulfurization and denitration technique and technique, using the heat in flue gas after the recovery denitration of oil cooling water cooling two-stage chilling technique.Device includes two grade cooling towers, is divided into oil wash section and washing section in tower, and two sections set spray thrower respectively, drawing pump, heat exchanger, recycle oil and circulating water outlet, recycle oil and recirculated water supply port, and flue gas riser and catch box are set between two sections.The present invention develops big for vapor and discharge quantity of particulate matter in existing flue gas desulfurization and denitration technique technology, the situation that heat significantly loses, oil wash is set to wash two grade cooling towers after denitrification apparatus, realize that flue gas heat reclaims, the consumption of water vapour in flue gas is farthest reduced simultaneously, and the continuous operation and energy-saving and emission-reduction for follow-up desulfurizer are significant.
Description
Technical field
The invention belongs to energy conservation project technical field, the heat reclaim unit and work being related in a kind of flue gas desulfurization and denitration technique
Skill, using the heat in flue gas after oil cooling-water cooling two-stage chilling technique recovery denitration.
Background technology
In fired coal combustion and crude oil production process, part sulphur and nitrogen are changed into SOXAnd NOX, air is discharged into flue gas,
Cause the pollution to environment so that flue gas pollutant emission control is extensively concerned, denitrating flue gas desulfurization technology also mature.
The gas denitrifying technology of selective catalytic reduction (SCR) has become high in the world because its denitration efficiency is high, market prospects are good
The first choice of effect control discharged nitrous oxides.In 320~380 DEG C of temperature ranges, reducing agent ammonia is in aerobic condition and catalysis
In the presence of agent, reduction reaction selectively occurs with NOx, generates N2And H2O.Flue gas desulfurization technique can be divided into wet method, dry method
With three kinds of semidry method, Wet Flue Gas Desulfurization Technique cardinal principle is to utilize the SO in alkaline absorption solution removing flue gasX.Due to wet method cigarette
Desulfurization technology desulfurization degree may be up to 95%, and plant running reliability is high, and simple to operate, processing cost is low, therefore each in the world
At present in existing flue gas desulfurization technique, dominant position is occupied in wet desulphurization for state.
During SCR denitration-wet desulfurizing process, temperature enters up to 140 DEG C -200 DEG C after denitration exiting flue gas dedusting
It is about 50 DEG C -60 DEG C that wet desulphurization device alkalies, which absorbs temperature, the loss of a large amount of moisture discharges, at the same in flue gas particulate matter with
Moisture discharge causes serious atmosphere pollution into air." the army et.al of Zhao Lv Ming, import is reduced in wet desulfurization system
The reduction of desulfurization entrance flue gas temperature is pointed out in the analysis and experiment of flue-gas temperature water saving ", desulphurization system water consumption can be significantly reduced
Amount, but it is used only heat exchanger and exchanged heat for inlet flue gas, and gas phase heat exchange area is big, and influences flue gas flow rate after heat exchanger cooling,
And then influence desulfurization alkali liquor absorption efficiency.Therefore heat reclaim unit is set significantly to drop between denitrification apparatus and desulfurizer
Low flue gas desulfurization temperature, so as to reduce desulfurizer vapor and particulate pollutant discharge capacity.The A of patent CN 105169795 are public
Opened it is a kind of can simultaneously denitration desulfurization two-stage chilling scrubber, including washing chilling area and alkali lye scrubbing section, flue gas pass through water
Wash after cooling again through alkali liquid washing desulphurization denitration, although its concise in technology, no longer needs thereafter desulfurization, the desulfurization simultaneously of its alkali lye
Denitration consumption is big, and flue gas heat can not recycle, and is not suitable for conventional flue gas desulfurization and denitrification.
The content of the invention
It is an object of the invention to provide the heat reclaim unit in a kind of flue gas desulfurization and denitration technique and technique.Flue gas takes off
The grade cooling tower of oil wash-washing two is set before desulfurizer after nitre device, heat and vapor in recovered flue gas, reduces particle
Thing discharges.
The technical solution adopted by the present invention is：
A kind of heat reclaim unit in flue gas desulfurization and denitration technique, including cooling tower, the cooling tower are cut-off up and down
Two grade cooling towers, subordinate's oil wash section and higher level's washing section are divided into two grade cooling towers, flue gas liter is set between two grade cooling towers
Tracheae；
Higher level's washing section internal upper part installs spray thrower, and circular water replenishing mouth is formed with higher level's washing section top, for being passed through spray
Leaching water, bottom sets circulating water outlet, and for discharging shower water, circulation is connected between circular water replenishing mouth and circulating water outlet
Water- to-water heat exchanger, for exchanging heat.Circulating water outlet is connected with circulating water regeneration system, and flue gas gas port is formed with the top of higher level's washing section,
It is connected with desulfurizer air inlet；
Subordinate's oil wash section internal upper part installation spray thrower, top side wall are formed with flue gas riser, and gas is drained into higher level's water
Section is washed, circulation repairing mouth is formed with subordinate's oil wash section top, for being passed through spray oil, bottom sets circulation oil export, is used for
Spray oil is discharged, the connection circulation oil heat exchanger between circulation repairing mouth and circulation oil export, for exchanging heat, bottom of towe recycle oil goes out
Mouth is connected with recycle oil regenerative system, and be formed with smoke air inlet in subordinate's oil wash pars infrasegmentalis is connected with denitrification apparatus gas outlet.
A kind of heat recovery technique in flue gas desulfurization and denitration technique, step are as follows
(1) denitration flue gas enters oil wash section from two-stage cooling tower bottom, and recycle oil is by way of directly spraying, with flue gas
Reverse contact heat-exchanging, the heat of higher temperatures section in flue gas is obtained, recycle oil is extracted out from bottom of towe, and a part is changed with circulation oil heat exchanger
Heat, a part remove recycle oil regenerative system, and clean makeup oil enters oil wash section from recycle oil return port, supplement the oil steaming of loss
Vapour and the contaminated oil extracted out；
(2) the flue gas of heat is tentatively taken through recycle oil by the air inlet between being arranged on two grade cooling towers, into washing section,
By the further reverse contact heat-exchanging of Water spray and flue gas, the oil vapour and vapor in flue gas are trapped, recycle oil is reduced and follows
The evaporation consumption of ring water；Recirculated water is collected by oil sump tank, the lateral line withdrawal function from tower, and a part exchanges heat with Heat Exchanger in Circulating Water System,
A part goes circulating water regeneration system, and supplement water enters washing section from recirculated water return port, supplements water vapour and the extraction of loss
Contaminant water, tower top outlet flue gas enters follow-up desulfurizer.
Moreover, the denitration flue-gas temperature is 140 DEG C -380 DEG C, oil wash section air outlet temperature is 90 DEG C~200 DEG C, washing section
Air outlet temperature is 40 DEG C~80 DEG C, and it is 100 DEG C -150 DEG C that circulation oil heat exchanger, which takes hot temperature, and Heat Exchanger in Circulating Water System takes the hot temperature to be
50℃-80℃。
Moreover, the oil mass for removing recycle oil regenerative system accounts for the 0.1%-80% of system circulation oil mass, supplement oil mass is
Go recycle oil regenerative system oil mass 1 times -1.5 times, the water of circulating water regeneration system is gone to account for the 0.1%- of system circulation water
80%, amount of makeup water is 1 times -1.2 times of circulating water regeneration system water.
Moreover, one-component or mixing oil product that it is 100 DEG C~480 DEG C that the cooling oil, which is boiling temperature, and boiling range
For 130 DEG C~450 DEG C distillations oil and coal liquifaction etc..
Moreover, two grade cooling tower uses void tower or number of theoretical plate as 1-40 blocks.
The device have the advantages that：
The present invention is big for vapor in existing flue gas desulfurization and denitration technique technology and discharge quantity of particulate matter, and heat significantly damages
The situation of mistake, the grade cooling tower of oil wash-washing two is set after denitrification apparatus, realizes that flue gas heat reclaims, recycle oil high-grade heat
It can be that miscellaneous equipment heats, while farthest be lowered into the amount of water vapour and particulate matter in the flue gas of desulfurizer.It is right
It is significant in the continuous operation and energy-saving and emission-reduction of follow-up desulfurizer.
Brief description of the drawings
Fig. 1：Heat reclaim unit in flue gas desulfurization and denitration technique.
Label declaration：1st, two grade cooling tower；2nd, oil wash section, 3, washing section；4th, oil heat exchanger is circulated；5th, recirculated water exchanges heat
Device；6th, denitration flue gas；7th, recycle oil；8th, recirculated water；9th, flue gas is discharged；10th, makeup oil；11st, water is supplemented；12nd, flue gas riser；
Embodiment
A kind of heat reclaim unit in flue gas desulfurization and denitration technique, including cooling tower 1, the cooling tower are cut-off up and down
Two grade cooling towers, be divided into subordinate's oil wash section 2 and higher level's washing section 3 in two grade cooling towers, flue gas be set between two grade cooling towers
Riser；
Higher level's washing section internal upper part installs spray thrower, and circular water replenishing mouth is formed with higher level's washing section top, for being passed through spray
Leaching water, bottom sets circulating water outlet, and for discharging shower water, circulation is connected between circular water replenishing mouth and circulating water outlet
Water- to-water heat exchanger 5, for exchanging heat.Circulating water outlet is connected with circulating water regeneration system, and flue gas gas port is formed with the top of higher level's washing section,
It is connected with desulfurizer air inlet.
Subordinate's oil wash section internal upper part installation spray thrower, top side wall are formed with flue gas riser, and gas is drained into higher level's water
Section is washed, circulation repairing mouth is formed with subordinate's oil wash section top, for being passed through spray oil, bottom sets circulation oil export, is used for
Spray oil is discharged, the connection circulation oil heat exchanger 4 between circulation repairing mouth and circulation oil export, for exchanging heat.Bottom of towe recycle oil
Outlet is connected with recycle oil regenerative system, and be formed with smoke air inlet in subordinate's oil wash pars infrasegmentalis is connected with denitrification apparatus gas outlet.
With reference to said apparatus, the flow of flue gas desulfurization and denitration technique is as follows in the present invention, with reference to accompanying drawing, illustrates operating procedure
It is as follows：
(1) denitration flue gas 6 enters oil wash section 2 from the bottom of towe of two grade cooling tower 1, and recycle oil is by way of directly spraying, with cigarette
The circulation of vital energy in the wrong direction obtains the heat of higher temperatures section in flue gas, recycle oil 7 is extracted out from bottom of towe, a part of to be exchanged heat with recycle oil to contact heat-exchanging
Device 4 exchanges heat, and a part removes recycle oil regenerative system, and clean makeup oil 10 enters oil wash section, supplement damage from recycle oil return port
The oil vapour of mistake and the contaminated oil extracted out.
(2) the flue gas of heat is tentatively taken through recycle oil by the flue gas riser 12 between being arranged on two grade cooling towers, into water
Section 3 is washed, by the further reverse contact heat-exchanging of Water spray and flue gas, the oil vapour and vapor in flue gas is trapped, reduces circulation
The evaporation of oil and recirculated water consumes；Recirculated water 8 is collected by oil sump tank, the lateral line withdrawal function from tower, and a part exchanges heat with recirculated water
Device 5 exchanges heat, and a part goes circulating water regeneration system, and clean supplement water 11 enters washing section, supplement damage from recirculated water return port
The water vapour of mistake and the contaminant water extracted out, tower top outlet flue gas 9 enter follow-up desulfurizer.
The temperature of denitration flue gas 6 is 140 DEG C -380 DEG C, and the air outlet temperature of oil wash section 2 is 90 DEG C~200 DEG C, and washing section 3 goes out
Temperature degree is 40 DEG C~80 DEG C, and it is 100 DEG C -150 DEG C that circulation oil heat exchanger 4, which takes hot temperature, and Heat Exchanger in Circulating Water System 5 takes the hot temperature to be
50℃-80℃.The oil mass of recycle oil regenerative system is gone to account for the 0.1%-80% of system circulation oil mass, supplement oil mass is to remove recycle oil
1 times -1.5 times of regenerative system oil mass, go the water of circulating water regeneration system to account for the 0.1%-80% of system circulation water, supplement
Water is 1 times -1.2 times of circulating water regeneration system water.
The cooling oil is the one-component that boiling temperature is 100 DEG C~480 DEG C or mixing oil product, and boiling range is 130
DEG C~450 DEG C of distillations oil and coal liquifaction etc..
Two grade cooling tower 1, because the gas phase of heat exchange is to contain SO2Hot-air, corrosivity is larger, and tolerance compared with
Greatly, quench oil is mostly easy foaming material, therefore two grade cooling tower mass transfer selection of internals are considered as the tower of corrosion resistance and the high F factors
Plate or structured packing.Oil wash section and washing section can use void tower or number of theoretical plate as 1-20 blocks.
Embodiment
The present embodiment illustrates the flue gas desulfurization and denitration technique of the present invention so that denitration treatment quantity is 50000 Nm3/h as an example
In heat reclaim unit, flue gas composition is as shown in table 1, concrete operation step and is described as follows：
The denitration flue gas of table 1 forms (volume fraction)：
| CO2 | 12% |
| O2 | 6% |
| N2 | 74.75% |
| SO2 | 0.25% |
| H2O | 7% |
140 DEG C of denitration flue gases 6 enter oil wash section 2 from the bottom of towe of two grade cooling tower 1, and 40 DEG C of recycle oils of 30t/h are by directly spraying
The mode of leaching, and the reverse contact heat-exchanging of flue gas, the heat of higher temperatures section in flue gas being obtained, 93 DEG C of recycle oils 7 are extracted out from bottom of towe,
29t/h recycle oils exchange heat with circulation oil heat exchanger 4, and 1t/h recycle oils go recycle oil regenerative system, makeup oil clean 1.1t/h
10 enter oil wash section from recycle oil return port, the contaminated oil supplemented the oil vapour of loss and extracted out.Heat is tentatively taken through recycle oil
Flue gas, temperature are 90 DEG C, enter washing section 3 by riser, further inversely contact is cooled to 40 to 60t/h Water sprays to flue gas
DEG C, trap the oil vapour and water vapour in flue gas.72 DEG C of recirculated waters 8 are collected by oil sump tank, the lateral line withdrawal function from tower, 59t/h
Exchanged heat with Heat Exchanger in Circulating Water System, 1t/h goes circulating water regeneration system, and supplement water 11 clean 1.3t/h enters from recirculated water return port
Enter washing section, the pollution water supplemented the water vapour of loss and extracted out.40 DEG C of flue gases 9 of tower top outlet enter desulfurizer.Tower top
Exiting flue gas composition is as shown in table 2
The tower top outlet flue gas of table 2 forms (volume fraction)：
| CO2 | 11.93% |
| O2 | 5.96% |
| N2 | 74.69% |
| SO2 | 0.21% |
| H2O | 7.21% |
Two-stage cooling tower tower top flue gas 9 carries out three-level alkali liquor absorption spray by desulfurizer, operation temperature in desulfurizing tower
40 DEG C, desulfurizing tower outlet drain flue gas composition using this patent desulfurizer outlet drain flue gas with not formed to the such as institute of table 3
Show, this patent is set before desulfurizer, desulfurization operations temperature can be reduced to 40 DEG C by 50 DEG C -60 DEG C, in desulfurization exiting flue gas
Water content can be down to 7.22% by 11.96%, significantly reduce the particle object amount of steam vapour amount and its entrainment.
The desulfurizer outlet drain flue gas of table 3 forms
| This patent is not used | Using this patent | |
| Gas forms | Volume fraction % | Volume fraction % |
| CO2 | 11.38% | 11.95% |
| O2 | 5.69% | 5.98% |
| N2 | 70.97% | 74.85% |
| SO2 | 0.00% | 0.00% |
| H2O | 11.96% | 7.22% |
Heat reclaim unit in flue gas desulfurization and denitration technique proposed by the present invention, entered by preferred embodiment
Gone description, person skilled substantially can not depart from present invention, in spirit and scope to structure as described herein and
Equipment is modified or suitably changed with combining, to realize the technology of the present invention.In particular, it is all similar to replace
Change and change it is apparent to those skilled in the art, they be considered as being included in spirit of the invention, scope and
In content.
Claims (6)
- A kind of 1. heat reclaim unit in flue gas desulfurization and denitration technique, it is characterised in that：Including cooling tower, the cooling tower is Two grade cooling towers separated up and down, it is divided into subordinate's oil wash section and higher level's washing section in two grade cooling towers, is set between two grade cooling towers Put flue gas riser；Higher level's washing section internal upper part installs spray thrower, and circular water replenishing mouth is formed with higher level's washing section top, is used for being passed through spray Water, bottom sets circulating water outlet, and for discharging shower water, connection recirculated water changes between circular water replenishing mouth and circulating water outlet Hot device, for exchanging heat.Circulating water outlet is connected with circulating water regeneration system, and flue gas gas port is formed with the top of higher level's washing section, with taking off Sulphur device air inlet connects；Subordinate's oil wash section internal upper part installation spray thrower, top side wall are formed with flue gas riser, and gas is drained into higher level's washing section, Circulation repairing mouth is formed with subordinate's oil wash section top, for being passed through spray oil, bottom sets circulation oil export, sprayed for discharging Leaching oil, the connection circulation oil heat exchanger between circulation repairing mouth and circulation oil export, for exchanging heat, bottom of towe circulates oil export with following Ring oil regeneration system is connected, and be formed with smoke air inlet in subordinate's oil wash pars infrasegmentalis is connected with denitrification apparatus gas outlet.
- 2. the heat recovery technique in the flue gas desulfurization and denitration technique that a kind of device using described in claim 1 is carried out, it is special Sign is：Step is as follows(1) denitration flue gas enters oil wash section from two-stage cooling tower bottom, and recycle oil is reverse with flue gas by way of directly spraying Contact heat-exchanging, the heat of higher temperatures section in flue gas being obtained, recycle oil is extracted out from bottom of towe, a part and circulation oil heat exchanger heat exchange, A part removes recycle oil regenerative system, and clean makeup oil enters oil wash section from recycle oil return port, supplements the oil vapour of loss With the contaminated oil of extraction；(2) tentatively take the flue gas of heat, into washing section, to pass through by the air inlet between being arranged on two grade cooling towers through recycle oil The further reverse contact heat-exchanging of Water spray and flue gas, traps the oil vapour and vapor in flue gas, reduces recycle oil and recirculated water Evaporation consumption；Recirculated water is collected by oil sump tank, the lateral line withdrawal function from tower, and a part exchanges heat with Heat Exchanger in Circulating Water System, one Divide circulating water regeneration system of going, supplement water enters washing section from recirculated water return port, the dirt for supplementing the water vapour of loss and extracting out Water is contaminated, tower top outlet flue gas enters follow-up desulfurizer.
- 3. technique according to claim 2, it is characterised in that：The denitration flue-gas temperature is 140 DEG C -380 DEG C, oil wash section Air outlet temperature be 90 DEG C~200 DEG C, washing section air outlet temperature be 40 DEG C~80 DEG C, circulation oil heat exchanger take hot temperature for 100 DEG C- 150 DEG C, it is 50 DEG C -80 DEG C that Heat Exchanger in Circulating Water System, which takes hot temperature,.
- 4. technique according to claim 2, it is characterised in that：The oil mass for removing recycle oil regenerative system accounts for system circulation The 0.1%-80% of oil mass, supplement oil mass are 1 times -1.5 times of recycle oil regenerative system oil mass, go circulating water regeneration system Water accounts for the 0.1%-80% of system circulation water, and amount of makeup water is 1 times -1.2 times of circulating water regeneration system water.
- 5. technique according to claim 2, it is characterised in that：The cooling oil is that boiling temperature is 100 DEG C~480 DEG C One-component or mixing oil product, and boiling range be 130 DEG C~450 DEG C distillation oil and coal liquifaction etc..
- 6. technique according to claim 2, it is characterised in that：Two grade cooling tower uses void tower or number of theoretical plate as 1- 40 pieces.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710565493.7A CN107388847A (en) | 2017-07-12 | 2017-07-12 | Heat reclaim unit and technique in flue gas desulfurization and denitration technique |
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| CN201710565493.7A CN107388847A (en) | 2017-07-12 | 2017-07-12 | Heat reclaim unit and technique in flue gas desulfurization and denitration technique |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108480381A (en) * | 2018-04-23 | 2018-09-04 | 天津大学 | A kind of organic polluted soil low energy consumption thermal desorption-adsorbing coupled restorative procedure of chilling- |
| CN108722124A (en) * | 2018-06-12 | 2018-11-02 | 昊姆（上海）节能科技有限公司 | The integral system and method for fair and clearization and waste heat recovery are taken off for smoke multistage |
| CN108970369A (en) * | 2018-10-09 | 2018-12-11 | 杭州蕴泽环境科技有限公司 | A kind of multisection type high-humidity gas fume device for deep cleaning and its purification process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5403569A (en) * | 1991-01-25 | 1995-04-04 | Abdelmalek; Fawzy T. | Process for boiler flue gas cleaning by absorption, separation and liquefaction |
| CN106178859A (en) * | 2016-08-22 | 2016-12-07 | 江苏中圣高科技产业有限公司 | Flue gas desulfurization fog dispersal haze system and method for sulfur recovery tail gas incinerator |
| CN205815447U (en) * | 2016-05-05 | 2016-12-21 | 济南冶金化工设备有限公司 | The double ammonia process integration desulfurization denitration system of coking flue gas two-part |
-
2017
- 2017-07-12 CN CN201710565493.7A patent/CN107388847A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5403569A (en) * | 1991-01-25 | 1995-04-04 | Abdelmalek; Fawzy T. | Process for boiler flue gas cleaning by absorption, separation and liquefaction |
| CN205815447U (en) * | 2016-05-05 | 2016-12-21 | 济南冶金化工设备有限公司 | The double ammonia process integration desulfurization denitration system of coking flue gas two-part |
| CN106178859A (en) * | 2016-08-22 | 2016-12-07 | 江苏中圣高科技产业有限公司 | Flue gas desulfurization fog dispersal haze system and method for sulfur recovery tail gas incinerator |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108480381A (en) * | 2018-04-23 | 2018-09-04 | 天津大学 | A kind of organic polluted soil low energy consumption thermal desorption-adsorbing coupled restorative procedure of chilling- |
| CN108722124A (en) * | 2018-06-12 | 2018-11-02 | 昊姆（上海）节能科技有限公司 | The integral system and method for fair and clearization and waste heat recovery are taken off for smoke multistage |
| CN108722124B (en) * | 2018-06-12 | 2023-02-28 | 昊姆（上海）节能科技有限公司 | Integrated system and method for multi-stage de-whitening purification and waste heat recovery of flue gas |
| CN108970369A (en) * | 2018-10-09 | 2018-12-11 | 杭州蕴泽环境科技有限公司 | A kind of multisection type high-humidity gas fume device for deep cleaning and its purification process |
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Application publication date: 20171124 |