CN205199299U - Active burnt gas cleaning system - Google Patents
Active burnt gas cleaning system Download PDFInfo
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- CN205199299U CN205199299U CN201521091096.3U CN201521091096U CN205199299U CN 205199299 U CN205199299 U CN 205199299U CN 201521091096 U CN201521091096 U CN 201521091096U CN 205199299 U CN205199299 U CN 205199299U
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- activated coke
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Abstract
The utility model provides an active burnt gas cleaning system, carries machine, storage silo and chimney including absorption regeneration integration purifying column, shale shaker, fill, it carries the machine intercommunication with chimney, shale shaker and fill respectively to adsorb regeneration integration purifying column, adsorb the inside from last to being adsorption stage, upper portion toper distributing device, the regeneration section of bleeding, regenerative heating section, regenerative cooling section and lower part toper distributing device down in proper order of the integrated purifying column of regeneration. The utility model discloses an integral structure accomplish to adsorb in a tower and regeneration, reduces active burnt loss, reduces the energy consumption, has high environmental protection, the high -efficient concurrent processing of multiple pollutant, advantages such as resources recovery, area are little, low energy consumption.
Description
Technical field
The utility model belongs to flue gases purification field, is specifically related to a kind of activated coke flue gas purification system.
Background technology
Produce a large amount of flue gas in the production engineerings such as coal-burning boiler, sintering, pelletizing, the SOx contained in flue gas, NOx, particle, heavy metal are with the materials such as bioxin are to environment.Along with national requirements for environmental protection increasingly stringent, the technology of the multiple contaminates thing comprehensive regulation is the inexorable trend of smoke gas treatment development.
Flue Gas Purification Technology Using Activated Coke, can realize low-temperature denitration on the basis of desulfurization, simultaneously to dust, heavy metal Ji the pollutants such as bioxin have certain removal effect.In addition, desulfurizing byproduct is high-quality sulfuric acid, can reclaim Sulphur ressource, meets the theory of recycling economy, is the multiple pollutant process for comprehensively treating of the most future that our times is generally acknowledged; But higher operating cost also limits applying of this technology.
Flue Gas Purification Technology Using Activated Coke is primarily of adsorption process and regenerative process composition, and the pollutant in adsorption process in flue gas is attracted to activated coke surface; In regenerative process, pollutant is from activated coke surface desorption, and activated coke realizes regeneration and recycles; Adsorptive reactor and activated coke regeneration reactor are the nucleus equipments of Flue Gas Purification Technology Using Activated Coke, exploitation multiple pollutant associated treatment, the absorption of low operating cost and regeneration reactor be the key of Flue Gas Purification Technology Using Activated Coke; The more process of current application is that adsorption tower and regenerator are arranged apart, as patent CN102430318 and patent CN104801174 individually discloses a kind of activated coke flue gas purification system, adsorption tower and regenerator arranged apart, activated coke cycles through many horizontal feed equipment and vertical transport equipment realizes, energy consumption is larger, and activated coke repeatedly batch turning cause loss comparatively large, thus add operating cost; Patent CN104785082 discloses a kind of absorption and regeneration Integral tower, and absorption and regeneration function can complete in a tower, but in this tower, pipeline is complicated, easily causes the uneven and locally accumulation of heat of activated coke blanking.
To sum up, existing activated coke adsorptive reactor and regeneration reactor and process exists flow process complexity, equipment is various, energy consumption is higher, activated coke blanking is uneven, the shortcomings such as easy accumulation of heat, need the absorption regeneration reactor developing new activated coke flue gas purifying technique and new construction, to reduce the loss of activated coke in running, and then reduce operating cost.
Summary of the invention
The purpose of this utility model is to provide a kind of activated coke flue gas purification system, small investment, take up an area little, flow process simple while, reach the effect of gas cleaning.
A kind of activated coke flue gas purification system that the utility model provides, comprises absorption regeneration integrated purifying tower, vibratory sieve, bucket elevator, storage bin and chimney; The exhaust outlet of absorption regeneration integrated purifying top of tower is communicated with chimney, the discharging opening of absorption regeneration integrated purifying tower bottom is communicated with by pipeline valve with the charging aperture of vibratory sieve, the bulky grain outlet of vibratory sieve is communicated with the charging aperture of bucket elevator, the discharging opening of bucket elevator is communicated with the charging aperture of absorption regeneration integrated purifying top of tower, being communicated with the charging aperture of bucket elevator of storage bin; The inside of absorption regeneration integrated purifying tower is followed successively by adsorption section, upper taper distributing device, the regeneration section of bleeding, regeneration bringing-up section, re-generatively cooled section and lower taper distributing device from top to bottom, is provided with medium lock air valve between upper taper distributing device and the regeneration section of bleeding.
In said system, the air inlet of adsorption section and the outlet of air blast, the pipeline that both are communicated with is communicated with water pipe with spray ammonia pipeline simultaneously.
In said system, upper taper distributing device is formed by multiple funnel is evenly distributed.
In said system, the regeneration section of bleeding is provided with the inlet communication of bleeding point and the first air-introduced machine.
In said system, regeneration bringing-up section is tubular heat exchanger, each tubulation inside is used for passing through activated coke, tubulation is communicated with re-generatively cooled section with the regeneration section of bleeding, shell is provided with hot wind inlet and return air outlet, the inlet communication of return air outlet and the second air-introduced machine, the outlet of the second air-introduced machine is all communicated with heater with the hot wind inlet of regeneration bringing-up section.
In said system, re-generatively cooled section is tubular heat exchanger, and each tubulation inside is used for by activated coke, and tubulation and regeneration bringing-up section are for be communicated with vibratory sieve, and shell is provided with hot-air evacuation port and inlet of cold air, the outlet of inlet of cold air and the 3rd air-introduced machine.
In said system, between bucket elevator and absorption regeneration integrated purifying tower, be provided with top blocking valve, between absorption regeneration integrated purifying tower and vibratory sieve, be provided with bottom blocking valve.
In said system, lower taper distributing device is formed by multiple funnel is evenly distributed.
The method of carrying out activated coke gas cleaning of activated coke flue gas purification system of the present utility model is adopted to be:
1, in adsorption section, fill activated coke, and in adsorption section, carry activated coke by bucket elevator;
2, by flue gas by entering the adsorption section lateral flow of absorption regeneration integrated purifying tower after blower, simultaneously pass into ammonia to adsorption section; SOx in adsorption section in flue gas, particle, heavy metal He bioxin are by activated coke Adsorption, and NOx and ammonia gas react generate nitrogen and water, and the flue gas after purification passes through smoke stack emission;
3, activated coke is after adsorption section completes absorption, the absorption saturated active coke formed flows downward, after upper taper distributing device, enter the regeneration section of bleeding, produce hot blast by heating devices heat air, be transferred to regeneration bringing-up section by the second air-introduced machine, with the heat exchange of absorption saturated active coke, activated coke is regenerated, formation regeneration activity is burnt, and the regenerative mixed gas of generation returns the regeneration section of bleeding, and is discharged by the first air-introduced machine;
4, regeneration activity Jiao enters re-generatively cooled section, and pass into air and the burnt heat exchange of regeneration activity by the 3rd air-introduced machine to re-generatively cooled section, the hot blast of generation is discharged;
5, cooled regeneration activity Jiao enters vibratory sieve through lower taper distributing device, separates the partially recycled of particle diameter <1.5mm through Vibration Screen, and remaining regeneration activity Jiao returns absorption regeneration integrated purifying tower by bucket elevator and recycles; Be transported in bucket elevator by the activated coke stored in storage bin, Jiao mixes with regeneration activity, the activated coke of replenish lost simultaneously.
In said method, by regulating the top blocking valve between bucket elevator and absorption regeneration integrated purifying tower and the medium lock air valve in absorption regeneration integrated purifying tower, prevent flue gas excessive, and isolated air; By regulating the bottom blocking valve between absorption regeneration integrated purifying tower and vibratory sieve and the medium lock air valve in absorption regeneration integrated purifying tower to maintain the air-tightness of regenerative process.
Above-mentioned flue-gas temperature is 80 ~ 180 DEG C; When flue-gas temperature >=140 DEG C, first flue gas is mixed with cold air, then be transferred in pipeline by booster fan, control the temperature < 140 DEG C entering the flue gas of adsorption section; When flue-gas temperature temperature >=160 DEG C, first flue gas is mixed with cold air, then be transferred in pipeline by booster fan, and spray cooling in the duct, control the temperature < 140 DEG C entering the flue gas of adsorption section.
SO in above-mentioned flue gas
2concentration be 500 ~ 1500mg/Nm
3, NOx is with NO
2the concentration of meter is 200 ~ 350mg/Nm
3, the concentration of particle is 50 ~ 100mg/Nm
3the concentration of ， bioxin is 1 ~ 5ng-TEQ/Nm
3.
In above-mentioned step 1, SO in the flue gas after purification
2concentration≤50mg/Nm
3; Concentration≤the 30mg/Nm of particle
3; Concentration≤the 100mg/Nm of NOx
3; Concentration≤the 0.5ng-TEQ/Nm of bioxin
3; Flue-gas temperature after purification is 130 ~ 140 DEG C.
In above-mentioned step 2, the amount passing into ammonia to adsorption section by the NOx complete reaction in ammonia and flue gas and excessive 0.5 ~ 1.5 times be as the criterion, the reaction equation of institute's foundation is:
4NO+4NH
3+O
2=4N
2+6H
2O
With
2NO
2+4NH
3+O
2=3N
2+6H
2O。
In above-mentioned step 2, the adsorption time of flue gas and activated coke is 30 ~ 60s, and the flow velocity of flue gas is 0.2 ~ 0.5m/s.
In above-mentioned step 3, SO in regenerative mixed gas
2percent by volume be 10 ~ 20%, be transferred in sulphuric acid plant for making sulfuric acid through the first air-introduced machine.
In above-mentioned step 2, the time of staying of activated coke in adsorption section is 7 ~ 10 days.
In above-mentioned step 3, the temperature of hot blast is 450 ~ 500 DEG C, and after hot blast enters regeneration bringing-up section and adsorbs saturated active coke heat exchange, the temperature of absorption saturated active coke is 350 ~ 420 DEG C, completes regeneration; Absorption saturated active coke is 2 ~ 3 hours in the time of staying of regeneration bringing-up section.
In above-mentioned step 4, after regeneration activity Jiao enters the heat exchange of re-generatively cooled section, temperature is 50 ~ 100 DEG C, and regeneration activity is burnt is 1 ~ 2 hour in the time of staying of re-generatively cooled section.
Principle of the present utility model and feature are:
Adopt integral structure, in a tower, complete absorption and regeneration, reduce the loss of activated coke, reduce activated coke loss and energy consumption, horizontal feed equipment and vertical-lift equipment can be reduced, obviously reduce system cloud gray model expense; In activated coke cyclic process, wearing and tearing produce coke powder, coke powder can slow down the translational speed of activated coke in absorption regeneration integrated purifying tower, cause activated coke to flow not smooth, therefore the short grained activated coke that Vibration Screen separates is set, and in system, supplements fresh activated coke by storage bin; Air-tightness in tower is maintained by regulating three blocking valves; When multiple absorption regeneration integrated purifying tower parallel operation, regulate adsorption section terminal valve, can voltage stabilizing be played used; Two conic distributors are set in absorption regeneration integrated purifying tower, can effectively activated coke flowing in control tower, realize bed of material Uniform Movement, prevent local stream not smooth; Technology and system method of the present utility model has high in environmental protection, the efficient associated treatment of multiple pollutant, the advantages such as resource reclaim, floor space are little, low energy consumption.
Accompanying drawing explanation
Fig. 1 is activated coke flue gas purification system structural representation of the present utility model;
In figure: 1-absorption regeneration integrated purifying tower, 2-top blocking valve, 3-medium lock air valve, blocking valve bottom 4-, 5-vibratory sieve, 6-bucket elevator, 7-valve III, 8-air blast, 9-water pipe, 10-valve I, 11-sprays ammonia pipeline, 12-valve II, 13-first air-introduced machine, 14-sulphuric acid plant, 15-second air-introduced machine, 16-heater, 17-the 3rd air-introduced machine, 18-chimney, 19-storage bin, 101-adsorption section, 102-upper taper distributing device, 103-regenerates the section of bleeding, 104-regenerates bringing-up section, 105-re-generatively cooled section, 106-lower taper distributing device,
Fig. 2 is the upper taper distributing device structural representation in the utility model embodiment;
Fig. 3 is that figure is cutd open in the A-A face of Fig. 2;
Fig. 4 is the tubular heat exchanger horizontal cross-section schematic diagram in the utility model embodiment.
Detailed description of the invention
Flue gas in the utility model embodiment is boiler smoke, sinter fume or pelletizing flue gas.
Ammonia gas volume concentrations in the utility model embodiment is 2.5 ~ 5%.
Ammonia pipeline is sprayed and ammonia gas generating device is assembled together in the utility model embodiment.
Acid preparation method in the utility model embodiment adopts GB50880-2013 normal pressure contact method acid-making process to carry out relieving haperacidity.
Heater in the utility model embodiment is heated by gas device or electric heater unit.
The structure that upper taper distributing device of the present utility model and lower taper distributing device are selected is formed by least 4 row and at least 4 row combinations by funnel, and the horizontal cross-section of each funnel is square, and plan structure as shown in Figure 2.
Embodiment 1
A kind of activated coke flue gas purification system structure as shown in Figure 1, comprises absorption regeneration integrated purifying tower 1, vibratory sieve 5, bucket elevator 6, storage bin 19 and chimney 18; The exhaust outlet at absorption regeneration integrated purifying tower 1 top is communicated with by valve II 12 with chimney 18, discharging opening bottom absorption regeneration integrated purifying tower 1 is communicated with by pipeline valve (bottom blocking valve 4) with the charging aperture of vibratory sieve 5, the bulky grain outlet of vibratory sieve 5 is communicated with the charging aperture of bucket elevator 6, the discharging opening of bucket elevator 6 is communicated with the charging aperture at absorption regeneration integrated purifying tower 1 top, being communicated with the charging aperture of bucket elevator 6 of storage bin 19; The inside of absorption regeneration integrated purifying tower 1 is followed successively by adsorption section 101, upper taper distributing device 102, the regeneration section of bleeding 103, regeneration bringing-up section 104, re-generatively cooled section 105 and lower taper distributing device 106 from top to bottom, is provided with medium lock air valve 3 between upper taper distributing device 105 and the regeneration section of bleeding 103;
The air inlet of adsorption section 101 and the outlet of air blast 8, the pipeline that both are communicated with is communicated with water pipe 9 with spray ammonia pipeline 11 simultaneously, and this pipeline is at spray ammonia pipeline connection place and be provided with valve I 10 between this pipeline and water pipe connectivity part; Be provided with arm with the pipeline of air blast 8 inlet communication, this arm is provided with valve III 7, and this arm is used for passing into cold air;
Upper taper distributing device 102 is formed by multiple funnel is evenly distributed, and structure as shown in Figures 2 and 3;
The regeneration section of bleeding 103 is provided with the inlet communication of bleeding point and the first air-introduced machine 13;
Regeneration bringing-up section 104 is tubular heat exchanger, horizontal cross-section structure as shown in Figure 4, each tubulation inside is used for passing through activated coke, tubulation is communicated with re-generatively cooled section 105 with the regeneration section of bleeding 103, shell is provided with hot wind inlet and return air outlet, the inlet communication of return air outlet and the second air-introduced machine 15, the outlet of the second air-introduced machine 15 is all communicated with heater 16 with the hot wind inlet of regeneration bringing-up section 104;
Re-generatively cooled section 105 is tubular heat exchanger, as shown in Figure 4, each tubulation inside is used for by activated coke horizontal cross-section structure, and tubulation is communicated with vibratory sieve 5 with regeneration bringing-up section 104, shell is provided with hot-air evacuation port and inlet of cold air, the outlet of inlet of cold air and the 3rd air-introduced machine 17;
Part beyond tubulation between regeneration bringing-up section 104 and re-generatively cooled section 105 is provided with thermal insulation board;
Be provided with top blocking valve 2 between bucket elevator 6 and absorption regeneration integrated purifying tower 1, between absorption regeneration integrated purifying tower 1 and vibratory sieve 5, be provided with bottom blocking valve 4;
Lower taper distributing device 106 is formed by multiple funnel is evenly distributed, identical with upper taper distributing device 102 structure;
The method adopting said system to carry out activated coke gas cleaning is:
1, in adsorption section, fill activated coke, and in adsorption section, carry activated coke by bucket elevator;
2, by flue gas by entering the adsorption section lateral flow of absorption regeneration integrated purifying tower after blower, simultaneously pass into ammonia to adsorption section; SOx in adsorption section in flue gas, particle, heavy metal are with the pollutants such as bioxin are by activated coke Adsorption, and NOx and ammonia gas react generate nitrogen and water, and the flue gas after purification passes through smoke stack emission;
3, activated coke is after adsorption section completes absorption, the absorption saturated active coke formed flows downward, after upper taper distributing device, enter the regeneration section of bleeding, add hot-air by heater 16 and produce hot blast, be transferred to regeneration bringing-up section by the second air-introduced machine, with the heat exchange of absorption saturated active coke, activated coke is regenerated, formation regeneration activity is burnt, and the regenerative mixed gas of generation returns the regeneration section of bleeding, and is discharged by the first air-introduced machine;
4, regeneration activity Jiao enters re-generatively cooled section, and pass into air and the burnt heat exchange of regeneration activity by the 3rd air-introduced machine to re-generatively cooled section, the hot blast of generation is discharged;
5, cooled regeneration activity Jiao enters vibratory sieve through lower taper distributing device, the part (active coke powder) separating particle diameter <1.5mm through Vibration Screen reclaims, and remaining regeneration activity Jiao returns absorption regeneration integrated purifying tower by bucket elevator and recycles; Be transported in bucket elevator by the activated coke stored in storage bin, Jiao mixes with regeneration activity, the activated coke of replenish lost simultaneously; Particles etc. are adsorbed by activated coke, by vibratory sieve, enter coke powder after screening;
By regulating the top blocking valve between bucket elevator and absorption regeneration integrated purifying tower and the medium lock air valve in absorption regeneration integrated purifying tower, prevent flue gas excessive, and isolated air; By regulating the bottom blocking valve between absorption regeneration integrated purifying tower and vibratory sieve and the medium lock air valve in absorption regeneration integrated purifying tower to maintain the air-tightness of regenerative process;
Flue-gas temperature is 80 ~ 180 DEG C; When flue-gas temperature >=140 DEG C, first flue gas is mixed with cold air, then be transferred in pipeline by booster fan, control the temperature < 140 DEG C entering the flue gas of adsorption section; When flue-gas temperature temperature >=160 DEG C, first flue gas is mixed with cold air, then be transferred in pipeline by booster fan, and spray cooling in the duct, control the temperature < 140 DEG C entering the flue gas of adsorption section;
SO in flue gas
2concentration be 500 ~ 1500mg/Nm
3, NOx is with NO
2the concentration of meter is 200 ~ 350mg/Nm
3, the concentration of particle is 50 ~ 100mg/Nm
3the concentration of ， bioxin is 1 ~ 5ng-TEQ/Nm
3;
SO in flue gas after purification
2concentration≤50mg/Nm
3; Concentration≤the 30mg/Nm of particle
3; Concentration≤the 100mg/Nm of NOx
3; Concentration≤the 0.5ng-TEQ/Nm of bioxin
3; Flue-gas temperature after purification is 130 ~ 140 DEG C;
The amount passing into ammonia to adsorption section by the NOx complete reaction in ammonia and flue gas and excessive 0.5 ~ 1.5 times be as the criterion;
The adsorption time of flue gas and activated coke is 30 ~ 60s, and the flow velocity of flue gas is 0.2 ~ 0.5m/s.SO in regenerative mixed gas
2percent by volume be 10 ~ 20%, be transferred in sulphuric acid plant 14 for making sulfuric acid through the first air-introduced machine; The time of staying of activated coke in adsorption section is 7 ~ 10 days; The temperature of hot blast is 450 ~ 500 DEG C, and after hot blast enters regeneration bringing-up section and adsorbs saturated active coke heat exchange, the temperature of absorption saturated active coke is 350 ~ 420 DEG C, completes regeneration; Absorption saturated active coke is 2 ~ 3 hours in the time of staying of regeneration bringing-up section; After regeneration activity Jiao enters the heat exchange of re-generatively cooled section, temperature is 50 ~ 100 DEG C, and regeneration activity is burnt is 1 ~ 2 hour in the time of staying of re-generatively cooled section.
Claims (6)
1. an activated coke flue gas purification system, is characterized in that comprising absorption regeneration integrated purifying tower, vibratory sieve, bucket elevator, storage bin and chimney; The exhaust outlet of absorption regeneration integrated purifying top of tower is communicated with chimney, the discharging opening of absorption regeneration integrated purifying tower bottom is communicated with by pipeline valve with the charging aperture of vibratory sieve, the bulky grain outlet of vibratory sieve is communicated with the charging aperture of bucket elevator, the discharging opening of bucket elevator is communicated with the charging aperture of absorption regeneration integrated purifying top of tower, being communicated with the charging aperture of bucket elevator of storage bin; The inside of absorption regeneration integrated purifying tower is followed successively by adsorption section, upper taper distributing device, the regeneration section of bleeding, regeneration bringing-up section, re-generatively cooled section and lower taper distributing device from top to bottom, is provided with medium lock air valve between upper taper distributing device and the regeneration section of bleeding.
2. a kind of activated coke flue gas purification system according to claim 1, is characterized in that the air inlet of described adsorption section and the outlet of air blast, and the pipeline that both are communicated with is communicated with water pipe with spray ammonia pipeline simultaneously.
3. a kind of activated coke flue gas purification system according to claim 1, is characterized in that the described regeneration section of bleeding is provided with the inlet communication of bleeding point and the first air-introduced machine.
4. a kind of activated coke flue gas purification system according to claim 1, it is characterized in that described regeneration bringing-up section is tubular heat exchanger, each tubulation inside is used for passing through activated coke, tubulation is communicated with re-generatively cooled section with the regeneration section of bleeding, shell is provided with hot wind inlet and return air outlet, the inlet communication of return air outlet and the second air-introduced machine, the outlet of the second air-introduced machine is all communicated with heater with the hot wind inlet of regeneration bringing-up section.
5. a kind of activated coke flue gas purification system according to claim 1, it is characterized in that described re-generatively cooled section is tubular heat exchanger, each tubulation inside is used for passing through activated coke, tubulation and regeneration bringing-up section are for be communicated with vibratory sieve, shell is provided with hot-air evacuation port and inlet of cold air, the outlet of inlet of cold air and the 3rd air-introduced machine.
6. a kind of activated coke flue gas purification system according to claim 1, is characterized in that being provided with top blocking valve between described bucket elevator and absorption regeneration integrated purifying tower, is provided with bottom blocking valve between absorption regeneration integrated purifying tower and vibratory sieve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521091096.3U CN205199299U (en) | 2015-12-25 | 2015-12-25 | Active burnt gas cleaning system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521091096.3U CN205199299U (en) | 2015-12-25 | 2015-12-25 | Active burnt gas cleaning system |
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| Publication Number | Publication Date |
|---|---|
| CN205199299U true CN205199299U (en) | 2016-05-04 |
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ID=55837044
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|---|---|---|---|
| CN201521091096.3U Expired - Fee Related CN205199299U (en) | 2015-12-25 | 2015-12-25 | Active burnt gas cleaning system |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105413326A (en) * | 2015-12-25 | 2016-03-23 | 中冶北方（大连）工程技术有限公司 | Active coke flue gas purifying system |
| CN107866142A (en) * | 2017-10-31 | 2018-04-03 | 中冶华天工程技术有限公司 | Disposal system for cement industry dry desulfurization denitration accessory substance |
| CN108525466A (en) * | 2018-05-09 | 2018-09-14 | 中国科学院过程工程研究所 | A kind of low-sulfur flue gas desulfurization and denitrification device |
| CN110180355A (en) * | 2019-06-10 | 2019-08-30 | 东营市俊源石油技术开发有限公司 | A kind of wet-dry change combined desulfurization and denitration running gear and method |
| CN112221301A (en) * | 2020-09-30 | 2021-01-15 | 武汉钢铁有限公司 | Activated carbon flue gas purification system and method thereof |
-
2015
- 2015-12-25 CN CN201521091096.3U patent/CN205199299U/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105413326A (en) * | 2015-12-25 | 2016-03-23 | 中冶北方（大连）工程技术有限公司 | Active coke flue gas purifying system |
| CN105413326B (en) * | 2015-12-25 | 2017-09-19 | 中冶北方（大连）工程技术有限公司 | A kind of activated coke flue gas purification system |
| CN107866142A (en) * | 2017-10-31 | 2018-04-03 | 中冶华天工程技术有限公司 | Disposal system for cement industry dry desulfurization denitration accessory substance |
| CN107866142B (en) * | 2017-10-31 | 2021-05-14 | 中冶华天工程技术有限公司 | A processing system that is used for cement trade dry process SOx/NOx control accessory substance |
| CN108525466A (en) * | 2018-05-09 | 2018-09-14 | 中国科学院过程工程研究所 | A kind of low-sulfur flue gas desulfurization and denitrification device |
| CN110180355A (en) * | 2019-06-10 | 2019-08-30 | 东营市俊源石油技术开发有限公司 | A kind of wet-dry change combined desulfurization and denitration running gear and method |
| CN112221301A (en) * | 2020-09-30 | 2021-01-15 | 武汉钢铁有限公司 | Activated carbon flue gas purification system and method thereof |
| CN112221301B (en) * | 2020-09-30 | 2022-12-23 | 武汉钢铁有限公司 | Activated carbon flue gas purification system and method thereof |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160504 Termination date: 20171225 |