CN107055486B - A kind of flue gas acid preparing process waste heat utilizes method - Google Patents
A kind of flue gas acid preparing process waste heat utilizes method Download PDFInfo
- Publication number
- CN107055486B CN107055486B CN201710218915.3A CN201710218915A CN107055486B CN 107055486 B CN107055486 B CN 107055486B CN 201710218915 A CN201710218915 A CN 201710218915A CN 107055486 B CN107055486 B CN 107055486B
- Authority
- CN
- China
- Prior art keywords
- bed
- flue gas
- heat exchanger
- outlet
- heat
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G3/00—Steam superheaters characterised by constructional features; Details of component parts thereof
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a kind of flue gas acid preparing process waste heats to utilize method, half SO2Flue gas mixes with air, after First Heat Exchanger, the heating of preposition heat exchanger, into the preposition bed of SO 2 converter, after outlet sets heat exchanger heat exchange before menstruation, with the other half SO2After flue gas mixing, into first segment bed；First segment bed outlet is after the heat exchange of the first steam superheater, into second segment bed；Second segment bed outlet enters third section bed after the heat exchange of third heat exchanger；Third section bed outlet is after the heat exchange of the second steam superheater, and a part of outlet exchanges heat through First Heat Exchanger, another part outlet exchanges heat through the second heat exchanger, subsequently enters high temperature absorption tower；Tower outlet enters the 4th section of bed after the 4th heat exchanger and the heating of third heat exchanger；4th section of bed outlet is after third steam superheater and the heat exchange of the 4th heat exchanger, into final absorption tower.The Technological adaptability of this method is wide in range, easy to operate, reliable for operation, and waste heat utilization is high.
Description
Technical field
The invention belongs to technical field of inorganic chemical industry, and in particular to residual-heat utilization method during a kind of flue gas acid preparing.
Background technique
Currently, having put into the high concentration SO of industrialized production in non-ferrous metal oxygen-rich smelting flue gas acid preparing field2Flue gas turns
Change technology mainly has the pre- of the BAYQIK technology of Bayer A.G, the LUREC technology of Out-0tec and Meng Moke company, the U.S.
Transformation technology.These three technologies can handle φ (SO2The flue gas of) >=14%, and compared with routine transformation technique, specification of equipment subtracts
Small, operating cost reduces, heat recovery rate improves.Because Sulphur Dioxide must be converted at sulfur trioxide using multistage, conversion is changed
In thermal flow process, the cold air into converter heated need to reach specific temperature, and each section of air inlet is both needed to maintain optimum temperature, absorb
Tower air inlet need to be in optimum range.The heat exchange process of three kinds of above-mentioned high-concentration sulfur dioxide transformation technologies differs from one another, total
Though conversion ratio and absorptivity are high, there are device structure design requirement height, heat exchange process complexity, waste heat recovery plant failure wind for it
Danger height (waste heat boiler and economizer etc.), the problems such as heat energy utilization is unreasonable.Meanwhile by flue gas SO2Concentration adaptability, catalyst
The factors limitation such as performance and dosage, gas forms of distribution, operation control complexity, in the industrial production, above-mentioned three kinds of technologies
There is the bottleneck problem for influencing the stable operation at full capacity of equipment long period in various degree.
Therefore, the high concentration SO generated for oxygen-rich smelting and melting continuously2Flue gas acid preparing technology develops reasonable heat exchange
Process keeps each section of intake air temperature rationally adjustable, and reduction flow path resistance, high efficiente callback waste heat improve SO as far as possible2Total conversion,
Relieving haperacidity exhaust emissions concentration and total amount are reduced, is current problem to be solved.
Summary of the invention
In view of the above existing problems in the prior art, the present invention provides a kind of flue gas acid preparing process waste heats to utilize method, should
The Technological adaptability of method is wide in range, easy to operate, reliable for operation, and waste heat utilization is high.
Above-mentioned purpose is realized by following proposal:
A kind of flue gas acid preparing process waste heat utilizes method, which is characterized in that this method are as follows: SO2Flue gas is in parallel by two
Sulphur dioxide blower mean allocation simultaneously conveys, the SO of sulphur dioxide blower conveying2The air of flue gas and air blower conveying
Mixing, successively after First Heat Exchanger, the heating of preposition heat exchanger, into the preposition bed of SO 2 converter, before described
The outlet of bed is set after the preposition heat exchanger heat exchange, is conveyed with another sulphur dioxide blower heated through the second heat exchanger
SO2After flue gas mixing, into the first segment bed of SO 2 converter；The outlet of the first segment bed is through the first steam
After superheater heat exchange, into the second segment bed of SO 2 converter；The outlet of the second segment bed is through third heat exchanger
Enter the third section bed of SO 2 converter after heat exchange；The outlet of the third section bed exchanges heat through the second steam superheater
Afterwards, a part of outlet exchanges heat through the First Heat Exchanger heat exchange, another part outlet through second heat exchanger, with laggard
Enter high temperature absorption tower；The outlet on the high temperature absorption tower is successively laggard through the 4th heat exchanger and the third heat exchanger heating
Enter the 4th section of bed of SO 2 converter；The outlet of the 4th section of bed is successively through third steam superheater and described
After the heat exchange of 4th heat exchanger, into final absorption tower；First saturated vapor is used for after the first steam superheater heating
Industry dragging steam turbine or steam turbine generator；Second saturated vapor successively passes through the third steam superheater and the second steam
After superheater heating, it to be used for steam turbine generator.
Method is utilized according to above-mentioned flue gas acid preparing process waste heat, which is characterized in that the SO2In flue gas, SO2Volume hundred
Dividing specific concentration is 22~28%, O2Concentration of volume percent is 6.5~10%.
Method is utilized according to above-mentioned flue gas acid preparing process waste heat, which is characterized in that into the SO of SO 2 converter2
Amount of flue gas emission and air total amount constitute the total gas for entering SO 2 converter, and the oxygen sulphur ratio of total gas is 0.85~
0.90。
Method is utilized according to above-mentioned flue gas acid preparing process waste heat, which is characterized in that the preposition bed, first segment bed
Layer, second segment bed, third section bed, the 4th section of bed Sulphur Dioxide rate be respectively 68~70%, 74~76%, 90~
92%, 95~97%, 98~99.5%.
Method is utilized according to above-mentioned flue gas acid preparing process waste heat, which is characterized in that the preposition bed of Xiang Suoshu conveys SO2
The wind pressure that the sulphur dioxide blower of flue gas provides is identical as the wind pressure that air blower provides, and is higher than to the first segment bed
Convey SO2The wind pressure that the sulphur dioxide blower of flue gas provides.
Method is utilized according to above-mentioned flue gas acid preparing process waste heat, which is characterized in that the sulphur dioxide blower and air
Blower is driven by the coaxial dual drive system being made of motor and the industry dragging steam turbine, passes through freewheel clutch reality
The conversion of existing driving device.
According to above-mentioned flue gas acid preparing process waste heat utilize method, which is characterized in that first saturated vapor from
The high-temperature flue gas waste heat of melting outlet of still is arranged during continual copper smelting high-temperature flue gas waste heat boiler and blowing outlet of still setting
Boiler, the pressure of first saturated vapor are 4.0~4.2MPa.
According to above-mentioned flue gas acid preparing process waste heat utilize method, which is characterized in that second saturated vapor from
The low temperature heat recovery apparatus of dry matter translocation setting, the pressure of second saturated vapor are 0.8~1.0MPa.
Method is utilized according to above-mentioned flue gas acid preparing process waste heat, which is characterized in that the third section bed gas output
60~70% enter in the First Heat Exchanger, and the 30~40% of the gas output of the third section bed enter described second
In heat exchanger.
Beneficial effects of the present invention:
Flue gas acid preparing process waste heat of the invention can realize the flue gas flow and oxygen sulphur ratio into converter using method
Optimum Regulation, total volumetric flow rate is few, and gas distribution mode is efficient, and work done during compression needed for conveying is small, and power consumption is low；Can efficiently and utilize
Each section of reaction bed outlet waste heat, system heat balance are easy to keep and adjust；Waste heat is recycled using steam superheater, is improved
Low-pressure steam quality, acting ability are strong, and generating efficiency improves, while having evaded using failure existing for waste heat boiler, economizer
Risk provides safety guarantee for production stable operation；Using industry drag the direct Driving Fan of steam turbine, avoid thermal energy →
Loss in efficiency in electric energy → mechanical energy conversion process, improves waste heat utilization.
Detailed description of the invention
Fig. 1 is the flow diagram that flue gas acid preparing process waste heat of the invention utilizes method.
Specific embodiment
The present invention is according to the produced high concentration SO of continual copper smelting2The characteristics of flue gas, bases oneself upon sulfuric acid domestic manufacture of key equipment, provides one kind
The heat exchange process and Waste Heat Reuse method to match with the distribution of flue gas acid preparing conversion ratio, starts with from material balance and heat balance,
Reasonable distribution conversion ratio can determine that loadings according to catalyst performance, corresponding control measures be arranged, maintain best thermal balance shape
State makes oxygen sulphur be easier to reach the conversion ratio of setting than adjustable, each section of reaction bed of optimization, realize the dense tolerance adaptability of gas it is wide in range,
Easy to operate target easily-controllable, reliable for operation, waste heat utilization is high.
As shown in Figure 1, SO 2 converter of the invention includes preposition bed 1, first segment bed 2, second segment bed
3, third section bed 4, the 4th section of bed 5.SO2In flue gas, SO2Concentration of volume percent is 22~28%, O2Percent by volume is dense
Degree is 6.5~10%.Sulfur dioxide flue gas is after preposition bed 1, and into double-absorption process, double-absorption process uses " 3+1 "
The form of section conversion.Preposition bed, first segment bed, second segment bed, third section bed, the 4th section of bed sulfur dioxide turn
Rate is respectively 68~70%, 74~76%, 90~92%, 95~97%, 98~99.5%.A kind of flue gas acid preparing provided by the invention
Process waste heat utilizes method, high concentration SO purified, after drying2Flue gas is conveyed by two sulphur dioxide blower mean allocations,
One sulphur dioxide blower 6 conveys half flue gas, and the dry air sent out with air blower 7 mixes, successively through first after mixing
After heat exchanger 8, preposition heat exchanger 9 heat, into preposition bed 1.The other half dioxy of another sulphur dioxide blower 10 conveying
Change sulphur flue gas after the heating of the second heat exchanger 11, after mixing with 1 outlet of preposition bed for setting the heat exchange of heat exchanger 9 before menstruation, into two
Turn the two first segment beds 2 for inhaling process.That is, preposition bed outlet is used to heat the gas into preposition bed.First segment bed 2
Outlet through the first steam superheater 12 heat the first saturated vapor after, enter back into second segment bed 3.3 outlet of second segment bed
Enter third section bed 4 after the heat exchange of third heat exchanger 13.4 outlet of third section bed is through through the second steam superheater 14 heating the
After two steam, a part of outlet exchanges heat through First Heat Exchanger 8, another part outlet exchanges heat through the second heat exchanger 11, subsequently enters
High temperature absorption tower.That is, third section bed outlet is after the heat exchange of the second steam superheater, a part of outlet is for heating into preposition
The gas of bed, another part outlet are used to heat the sulfur dioxide flue gas into the first bed.Preferably, third section bed goes out
Tolerance 60~70% enters in First Heat Exchanger 8, and 30~40% enter in the second heat exchanger 11.High temperature absorption tower outlet is successively through
Four heat exchangers 15 and third heat exchanger 13 enter the 4th section of bed 5 after heating.The outlet of 4th section of bed 5 is successively through third steam
After superheater 16 and the heat exchange of the 4th heat exchanger 15, into final absorption tower.4th section of bed outlet is steamed for heating the second saturation
Vapour and high temperature absorption tower outlet.First saturated vapor is after the heating of the first steam superheater 12, and a part is for industry dragging vapour
Turbine, another part are used for steam turbine generator.Second saturated vapor successively passes through third steam superheater 16 and the second steam mistake
After hot device 14 heats, it to be used for steam turbine generator.Wherein, the first saturated vapor melting outlet of still during continual copper smelting is set
The high-temperature flue gas waste heat boiler of the high-temperature flue gas waste heat boiler and blowing outlet of still setting set, the pressure of the first saturated vapor are
4.0~4.2MPa.The low temperature heat recovery apparatus that second saturated vapor is arranged from dry matter translocation, the pressure of the second saturated vapor
For 0.8~1.0MPa.
First steam superheater, the second steam superheater and third steam superheater are utilized respectively flue gas acid preparing process and change
The waste heat of the waste heat of the first segment bed exit gas of thermal flow process, the 4th section of bed and third section bed exit gas, overheat connect
First steam of continuous copper metallurgy system production and the second steam of dry matter translocation low temperature exhaust heat recovery system production.Wherein the first saturation
After steam superheating, a part directly drives sulphur dioxide blower and air blower for industry dragging steam turbine, and another part is used
After power generation, the second saturated vapor overheat, it is directly used in power generation.
Industry dragging steam turbine directly drives sulphur dioxide blower and air blower, and reference is by industry dragging steam turbine and electricity
The coaxial dual drive system that motivation is constituted, driving device are mounted on blower two sides, configure freewheel clutch, pass through freewheel clutch
Realize the automatic conversion between driving device.When the original starting of blower or superheated steam pressure reduction and industry dragging steam turbine event
When barrier, industry drags steamer pusher side freewheel clutch automatic unbuckling, by motor drive blower；When industry dragging steam turbine work
When, motor side freewheel clutch automatic unbuckling.
Flue gas acid preparing process waste heat of the invention utilizes method, into the SO of SO 2 converter2Amount of flue gas emission and sky
Gas total amount constitutes the total gas for entering SO 2 converter, and the oxygen sulphur ratio of total gas is 0.85~0.90.Total gas has been determined
The oxygen sulphur ratio of body, further according to SO2Amount of flue gas emission, the amount for the air that determination need to be incorporated.
Particularly, SO is conveyed to preposition bed2What the wind pressure and air blower that the sulphur dioxide blower of flue gas provides provided
Wind pressure is identical, and is higher than to first segment bed and conveys SO2The wind pressure that the sulphur dioxide blower of flue gas provides.
With specific embodiment, invention is further explained below.
Embodiment 1
The high concentration SO that golden peak continual copper smelting system generates2In flue gas during smelting, SO2Concentration of volume percent 25.5VOL%, O2
Concentration of volume percent 8.5VOL%.High concentration SO after purified, dry2Flue gas during smelting by two parallel configurations titanium dioxide
Sulphur blower, which is divided equally, to be conveyed, and half flue gas is sent out by sulphur dioxide blower, and the dry air sent out with air blower mixes.Wherein,
Air amount of allocating is according to the oxygen sulphur of total gas than 0.88 and SO2Amount of flue gas emission is controlled.Mixed gas is successively through the first heat exchange
After device, the heating of preposition heat exchanger, into preposition bed, conversion ratio 69.5% is designed；Preposition bed outlet sets heat exchanger heat exchange before menstruation
It is uniformly mixed with the other half flue gas heated through the second heat exchanger sent out by sulphur dioxide blower afterwards, into double-absorption process
First segment bed, design conversion ratio 75%；One section of outlet removes heat, heating continual copper smelting melting through the first steam superheater
Waste heat boiler and blowing produced first saturated vapor of waste heat boiler, enter back into second segment bed, design conversion ratio 91%；Two sections
Outlet exchanges heat through third heat exchanger, into third section bed, designs conversion ratio 96%；Three sections of outlets are moved through the second steam superheater
Except partial heat, a part of gas (accounting for three sections of outlets 62%) enters First Heat Exchanger 8, and another part gas (accounts for three sections of outlets
38%) enter the second heat exchanger, after removing heat, into the high temperature absorption tower of dry matter translocation, high temperature absorption tower upper section outlet is through the
Enter the 4th section of bed after four heat exchangers, the heating of third heat exchanger, designs conversion ratio 99%；Four sections of outlets are through the second steam superheating
Device and the 4th heat exchanger enter final absorption tower after removing heat.Refining after conversion waste heat superheater from continuous is utilized in process
The high-temperature flue gas waste heat boiler of melting outlet of still is arranged during copper high-temperature flue gas waste heat boiler and blowing outlet of still setting
First saturated vapor a part directly drives sulphur dioxide blower and air blower for industry dragging steam turbine, and another part is used
Second saturated vapor of the low temperature heat recovery apparatus from dry matter translocation setting after power generation, overheat is directly used in power generation.
Claims (9)
1. a kind of flue gas acid preparing process waste heat utilizes method, which is characterized in that this method are as follows: SO2Flue gas is by two dioxies in parallel
Change sulphur blower mean allocation and conveys, the SO of sulphur dioxide blower conveying2Flue gas is mixed with the air that air blower conveys,
Successively after First Heat Exchanger, the heating of preposition heat exchanger, into the preposition bed of SO 2 converter, the preposition bed
Outlet after the preposition heat exchanger heat exchange, the SO that is conveyed with another sulphur dioxide blower heat through the second heat exchanger2
After flue gas mixing, into the first segment bed of SO 2 converter；The outlet of the first segment bed is through the first steam superheating
After device heat exchange, into the second segment bed of SO 2 converter；The outlet of the second segment bed exchanges heat through third heat exchanger
Enter the third section bed of SO 2 converter afterwards；The outlet of the third section bed through the second steam superheater heat exchange after,
A part of outlet exchanges heat through the First Heat Exchanger heat exchange, another part outlet through second heat exchanger, subsequently enters
High temperature absorption tower；The outlet on the high temperature absorption tower successively enters after the 4th heat exchanger and the third heat exchanger heating
4th section of bed of SO 2 converter；The outlet of the 4th section of bed is successively through third steam superheater and described
After the heat exchange of four heat exchangers, into final absorption tower；First saturated vapor is used for work after the first steam superheater heating
Industry drags steam turbine or steam turbine generator；Second saturated vapor successively passes through the third steam superheater and the second steam mistake
After hot device heating, it to be used for steam turbine generator.
2. flue gas acid preparing process waste heat according to claim 1 utilizes method, which is characterized in that the SO2In flue gas, SO2
Concentration of volume percent is 22~28%, O2Concentration of volume percent is 6.5~10%.
3. flue gas acid preparing process waste heat according to claim 1 utilizes method, which is characterized in that enter Sulphur Dioxide
The SO of device2Amount of flue gas emission and air total amount constitute the total gas for entering SO 2 converter, and the oxygen sulphur ratio of total gas is
0.85~0.90.
4. flue gas acid preparing process waste heat according to claim 1 utilizes method, which is characterized in that the preposition bed, the
One section of bed, second segment bed, third section bed, the 4th section of bed Sulphur Dioxide rate be respectively 68~70%, 74~
76%, 90~92%, 95~97%, 98~99.5%.
5. flue gas acid preparing process waste heat according to claim 1 utilizes method, which is characterized in that the preposition bed of Xiang Suoshu
Convey SO2The wind pressure that the sulphur dioxide blower of flue gas provides is identical with the wind pressure that air blower provides, and higher than to described the
One section of bed conveys SO2The wind pressure that the sulphur dioxide blower of flue gas provides.
6. flue gas acid preparing process waste heat according to claim 1 utilizes method, which is characterized in that the sulphur dioxide blower
With air blower by being driven by motor and the coaxial dual drive system that constitutes of industry dragging steam turbine, by surmount from
The conversion of clutch realization driving device.
7. flue gas acid preparing process waste heat according to claim 1 utilizes method, which is characterized in that first saturated vapor
The high temperature cigarette of melting outlet of still is arranged during continual copper smelting high-temperature flue gas waste heat boiler and blowing outlet of still setting
Gas waste heat boiler, the pressure of first saturated vapor are 4.0~4.2MPa.
8. flue gas acid preparing process waste heat according to claim 1 utilizes method, which is characterized in that second saturated vapor
From the low temperature heat recovery apparatus of dry matter translocation setting, the pressure of second saturated vapor is 0.8~1.0MPa.
9. flue gas acid preparing process waste heat according to claim 1 utilizes method, which is characterized in that the third section bed
Gas output 60~70% enters in the First Heat Exchanger, described in 30~40% entrance of the gas output of the third section bed
The second heat exchanger in.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710218915.3A CN107055486B (en) | 2017-04-06 | 2017-04-06 | A kind of flue gas acid preparing process waste heat utilizes method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710218915.3A CN107055486B (en) | 2017-04-06 | 2017-04-06 | A kind of flue gas acid preparing process waste heat utilizes method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107055486A CN107055486A (en) | 2017-08-18 |
| CN107055486B true CN107055486B (en) | 2019-03-12 |
Family
ID=59601631
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710218915.3A Active CN107055486B (en) | 2017-04-06 | 2017-04-06 | A kind of flue gas acid preparing process waste heat utilizes method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107055486B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108046221B (en) * | 2017-12-12 | 2020-10-02 | 中国恩菲工程技术有限公司 | Method for preparing acid by smelting flue gas |
| CN109704294A (en) * | 2019-03-08 | 2019-05-03 | 长沙有色冶金设计研究院有限公司 | The method of the highly concentrated conversion system heat cascade utilization of sulfuric acid |
| CN112723319B (en) * | 2021-01-05 | 2022-12-27 | 长沙有色冶金设计研究院有限公司 | High concentration of SO 2 Method for preparing sulfuric acid by flue gas separation pre-conversion |
| CN112629276A (en) * | 2021-01-13 | 2021-04-09 | 易门铜业有限公司 | Multi-grade waste heat gradient upgrading power generation system and method |
| CN112679996A (en) * | 2021-01-15 | 2021-04-20 | 无锡东恒新能源科技有限公司 | Carbon black production method capable of recycling resources |
| CN114572939A (en) * | 2022-04-01 | 2022-06-03 | 陕西莹钰化工设备有限公司 | Original SO2Technology for preparing sulfuric acid by partial pre-conversion |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105983331B (en) * | 2015-02-06 | 2018-06-08 | 上海东化环境工程有限公司 | Industrial sulfur-containing tail gas sulfur removal technology |
| CN105056744B (en) * | 2015-09-20 | 2017-09-12 | 山西长林能源科技有限公司 | A kind of flue gas waste heat recovery, desulfurization integrated technique and device |
| CN105909330B (en) * | 2016-04-14 | 2018-06-19 | 东南大学 | A kind of flue gas waste heat recovery and smoke processing system based on Organic Rankine Cycle |
-
2017
- 2017-04-06 CN CN201710218915.3A patent/CN107055486B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN107055486A (en) | 2017-08-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107055486B (en) | A kind of flue gas acid preparing process waste heat utilizes method | |
| CN206600833U (en) | Ensure the smoke waste heat utilization system of SCR denitration efficiency under a kind of underload | |
| CN201103894Y (en) | Saturated steam heating stove | |
| CN105318313B (en) | A kind of smoke waste heat utilization system based on SCR denitration device | |
| CN107120642A (en) | A kind of supercritical carbon dioxide CFBB heating system and heating means | |
| CN202484963U (en) | Quality improvement and gradual utilization system of waste heat of boiler smoke of heat-engine plant | |
| CN201884079U (en) | Heat regenerative system of steam turbine generator unit capable of utilizing waste heat of heat conducting oil furnace in calcination plant | |
| CN203549787U (en) | Single-pressure saturated vapor superheated boiler | |
| CN202024614U (en) | Cement production line waste heat generating system | |
| CN101706095B (en) | Method for recovering acid making waste heat | |
| CN104131849A (en) | Combined circulating power generating system and method combining natural gas, oxygen and pulverized coal combustion | |
| CN217356829U (en) | Catalytic oxidation system with multi-cold source waste heat grading recovery function | |
| CN109099498A (en) | It is a kind of to couple the technique and method for generating thermoelectricity decoupling by coal dust firing flue gas shunting | |
| CN207094595U (en) | A kind of supercritical carbon dioxide boiler heating system | |
| CN202630027U (en) | Device for utilizing smoke waste heat of boiler of thermal generator set | |
| CN202675253U (en) | Device for utilizing waste heat of smoke of thermal power generating unit boiler | |
| CN106368915A (en) | Tower-type solar energy and fuel coal complementary power generation system | |
| CN208312354U (en) | A kind of double reheat electricity generation system | |
| CN201501791U (en) | Industrial acid making waste heat recovery system | |
| CN203159420U (en) | System for reducing corrosion to tail heating surface of glass melter waste heat boiler | |
| CN201916891U (en) | Energy-saving overheating steamer | |
| CN206875996U (en) | Coke-oven plant's coke-stove gas utilizes and smoke processing system | |
| CN207035091U (en) | CFBB and recirculating fluidized bed combined cycle system | |
| CN206876003U (en) | Charcoal ink factory's calcining furnace waste heat comprehensive utilization system | |
| CN201672817U (en) | Comprehensive utilization device for water of carbon calcination furnace water jackets and tail gas afterheat of coal economizers |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |