CN100427391C - Tail gas treatment and reutilization for calcium carbide stove - Google Patents

Tail gas treatment and reutilization for calcium carbide stove Download PDF

Info

Publication number
CN100427391C
CN100427391C CNB200610141746XA CN200610141746A CN100427391C CN 100427391 C CN100427391 C CN 100427391C CN B200610141746X A CNB200610141746X A CN B200610141746XA CN 200610141746 A CN200610141746 A CN 200610141746A CN 100427391 C CN100427391 C CN 100427391C
Authority
CN
China
Prior art keywords
calcium carbide
carbide stove
stove exhaust
ammonia
processing
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.)
Expired - Fee Related
Application number
CNB200610141746XA
Other languages
Chinese (zh)
Other versions
CN1939840A (en
Inventor
李智钦
田继生
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ningxia Yinglite Chemicals Co Ltd
Original Assignee
Ningxia Yinglite Chemicals Co Ltd
Ningxia Yinglite Power Group Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Ningxia Yinglite Chemicals Co Ltd, Ningxia Yinglite Power Group Corp filed Critical Ningxia Yinglite Chemicals Co Ltd
Priority to CNB200610141746XA priority Critical patent/CN100427391C/en
Publication of CN1939840A publication Critical patent/CN1939840A/en
Application granted granted Critical
Publication of CN100427391C publication Critical patent/CN100427391C/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Abstract

A re-utilizing treatment of calcium carbide furnace tail gas is carried out by preparing synthetic ammonia, desulfurizing, denitrifying and obtaining ammonia sulfate by-product. Its advantages include low cost, simple process, no secondary-environmental pollution and waste circulating utilization.

Description

The processing of calcium carbide stove exhaust with utilize method again
Technical field
The invention belongs to environmental protection technical field, particularly relate to a kind of processing of calcium carbide stove exhaust and utilize method again.
Background technology
Furnace of calcium carbide can produce a large amount of flue gases in process of production, as containing the carbon monoxide more than 80% in the closed calcium carbide furnace flue gas, also contains a large amount of dust and small amount of nitrogen, hydrogen etc.At present, dust removal process is normally carried out in the processing of known calcium carbide flue gas earlier, directly discharges or be used as fuel then.
Calcium carbide production is a kind of high energy industry, near extensive calcium carbide manufacturing enterprise, often needs supporting large-scale electric power enterprise.The smoke waste gas that boiler, the kiln that industries such as electric power, chemical industry, metallurgy are generally used discharged contains a large amount of sulfurous gas etc., and atmosphere is caused serious pollution.At present, domestic lime/lime stone-gypsum the method that generally adopts is handled above-mentioned boiler smoke, lime/lime stone-gypsum method mainly be utilize lime or Wingdale can with the characteristics of sulfurous gas reaction, flue gas is carried out the wet desulphurization washing, reach the purpose of flue, the desulfurizing byproduct of this method is a gypsum, owing to be subjected to the restriction in quality product and market, often can not commercialization, can only abandon stacking by land occupation, form secondary pollution; Use the sodium hydroxide doctor treatment, the product by product can be recycled, but has the high shortcoming of desulphurization cost; Adopt synthesis of ammonia desulfurization, desulfuration byproduct can be recycled, but the synthetic ammonia sweetening agent need be provided by synthetic ammonia factory, has desulphurization cost height, sweetening agent transportation too, stores than problems such as difficulties.Chinese patent CN1600410 discloses a kind of " integral method and the equipment of the stack gas ammonia process of desulfurization and desulfurization product comprehensive utilization ", the ammonia process of desulfurization of employing to the effect that of this method, by product ammonium bisulfite and ammonium sulphite need the follow-up acid treatment that adds, the byproduct for treatment complex procedures, also need to solve the source problem that comes of ammonia, so the desulphurization cost height.
Summary of the invention
The objective of the invention is to overcome the defective of above-mentioned prior art, economy, a kind of processing of calcium carbide stove exhaust is provided and utilizes method again, this method is that calcium carbide stove exhaust is prepared into synthetic ammonia, synthetic ammonia is used further to desulfurization, the denitrogenation processing of stack gas, this method has solved the source problem that comes of ammonia in the flue gas desulfurization, technology is simple, and cost is low, non-secondary pollution.
Technical scheme of the present invention is as follows:
A kind of processing of calcium carbide stove exhaust with utilize method again, it is characterized in that this method comprises the steps: the preprocessing process of calcium carbide stove exhaust, the tail gas synthetic ammonia process, the absorption of ammonia and course of conveying, ammoniacal liquor flue gas desulfurization, denitrification process, the doctor solution treating processes, wherein
The preprocessing process of described calcium carbide stove exhaust comprises cooling, dedusting and the scavenging process of calcium carbide stove exhaust;
Described tail gas synthetic ammonia process adopts the multistage conversion process that CO is transformed into H 2, conversion gas removes CO 2With produce N 2Adopt pressure swing adsorption technique, synthetic ammonia adopts middle-pressure process;
The absorption of described ammonia and course of conveying are that water absorbs ammonia, make ammoniacal liquor, by pump delivery and be used for boiler flue gas desulfurization, denitrogenation;
Described ammoniacal liquor flue gas desulfurization, denitrification process are after flue gas advances people's thionizer, contact with the whitewashing that comprises the ammoniacal liquor slurries, generate ammonium sulphite, the NO in ammonium sulphite and the flue gas 2Reaction generates ammonium sulfate and N 2Be oxidized to ammonium sulfate in the oxidation trough of unnecessary subsequently ammonium sulphite in being provided in thionizer, the xln content 3~4% of ammonium sulfate in the control doctor solution;
The doctor solution treating processes is meant that ammonium sulfate is made for standard compliant chemical fertilizer product after concentrated, crystallization, dehydration;
The cooling of described calcium carbide stove exhaust is meant calcium carbide stove exhaust sent in the byproduct steam boiler lowers the temperature;
Described dust removal process is to realize in the one-level multi-tube dust cleaner;
Described scavenging process is to adopt washing cooling, caustic wash desulfuration, and the tail gas CO purity after the purification reaches more than 90%;
Described CO conversion process is realized by 4 sections conversion;
Described separation of C O 2With produce N 2Adopt molecular sieve transformation suction type;
Above-mentioned unstripped gas after conversion and decarburization also need be removed CO and CO with the method for methanation behind the first methanolizing 2
Described synthetic ammonia pressure-controlling is at 30~40MPa.
Above-mentioned finish the ammonia absorption process after, residual gas is reentered ammonia synthesis converter and is reacted;
The doctor solution pH value is controlled at 6.5~7.0 in described ammoniacal liquor flue gas desulfurization, the denitrification process.
The present invention has following technical characterstic:
1. on the process for cooling of calcium carbide flue gas, considered to utilize the high-temperature flue gas waste heat, byproduct steam;
2. the calcium carbide flue gas adopts multi-tube dusting earlier, washes with water, has improved dust removing effects;
3. on synthetic gas removing carbon dioxide and nitrogen production by air separation technology, adopt pressure swing adsorption technique, simplified production technique;
4. the mixed gas separation behind the synthetic ammonia adopts water to absorb the ammonia separating technology, and technology is simple, energy efficient;
5. with depleted calcium carbide flue gas synthetic ammonia, production cost is low;
6. ammoniacal liquor directly send power plant to be used for flue gas desulfurization, denitrogenation, and price is low, and has reduced transportation, the storage cost of liquefied ammonia;
7. ammonium sulphite direct oxidation in thionizer generates ammonium sulfate, has simplified the treatment process of desulfuration byproduct;
8. the byproduct of ammonium sulfate deep processing becomes composite chemical fertilizer to sell.
Method of the present invention utilizes the ammonia of calcium carbide stove exhaust preparation to handle desulfurization, the denitrogenation problem of boiler smoke, solve the ammonia in the flue gas desulfurization and come source problem, desulphurization cost is low, the generation of non-secondary pollution problem, this method not only can realize the recycling of calcium carbide stove exhaust, reduce the pollution of calcium carbide stove exhaust to environment, can administer the pollution of the sulfurous gas, oxynitride of (power plant) flue gas again to environment, simultaneously can also produce chemical fertilizer product ammonium sulfate, reach the treatment of wastes with processes of wastes against one another, reduce and control useless cost, realize the cyclic utilization of waste.
Embodiment
1. the preprocessing process of calcium carbide stove exhaust, comprise calcium carbide stove exhaust cooling, dedusting and scavenging process, wherein
Temperature-fall period is meant with blower fan calcium carbide stove exhaust to be sent in the byproduct steam boiler lowers the temperature, and this process can produce 1.3~1.5MPa middle pressure steam;
Dust removal process is to realize at the one-level multi-tube dust cleaner;
Scavenging process is to adopt washing cooling, caustic wash desulfuration, is about to flue gas again by water wash column, soda-wash tower, removes grit, tar, CO 2, impurity such as sulphur, the tail gas CO purity after the purification reaches more than 90%.
2, tail gas synthetic ammonia process process adopts the multistage conversion process that CO is transformed into H 2, conversion gas removes CO 2With produce H 2Adopt the molecular sieve pressure swing adsorption technique, synthetic ammonia adopts middle-pressure process, is specially:
Tail gas CO and water vapor are for conversion into the needed feed hydrogen of synthetic ammonia under the effect of catalyzer.Reaction formula: CO+H 2O → H 2+ CO 2+ 41.2KJ; Because the content height of CO needs to consider four sections reactions that by conversion, the content of CO is reduced to about 0.5%;
CO in the conversion gas 2Adopt the mode of molecular sieve transformation absorption to remove;
Unstripped gas after conversion and decarburization still has a spot of CO (<0.5%) and CO 2(<0.1%) in order to prevent their poisonings to ammonia synthesis catalyst, need do purifying treatment, promptly adopts the method for methanation behind the first methanolizing, removes CO and CO 2
System nitrogen: adopt the molecular sieve adsorption separating technology with airborne oxygen and nitrogen separation system nitrogen;
Synthetic ammonia: adopt middle-pressure process, working pressure is 30~40MPa, and hydrogen and nitrogen are pressed certain proportioning raw materials mixed gas, and the compressed extremely synthetic pressure that needs adopts no oil pressure to contract, and can solve pressurized gas band oil problem.After hydrogen nitrogen mixed gas after the compression need be heated to the initial activity temperature of catalyzer, enter catalyst layer and carry out ammonia synthesis reaction.
3. the absorption of ammonia and course of conveying: from the gas mixture that synthetic tower comes out, ammonia content is 10~20%, and the method that adopts water to absorb is absorbed as ammoniacal liquor with ammonia, and ammonia concn is 15%, then by pump delivery and as (power plant) boiler flue gas desulfurization, denitrogenation.
After finishing the ammonia absorption process, residual gas also contains a large amount of unreacted hydrogen and nitrogen, and this part gas converges as circulating reaction gas and fresh synthesis gas, reenters ammonia synthesis converter and reacts.Recycle compressor is set on stream.
By way continuous or emptying at intermittence, the rare gas element in the circulation gas is discharged.
Because the synthesising reacting heat of CO transformation and hydrogen production and ammonia is bigger, can be used as the preceding hydrogen nitrogen mixed gas of 1. pre-thermal response; 2. heat hot water; 3. preboiler feedwater; 4. byproduct steam.
4, ammoniacal liquor desulfurization, denitrification process comprise three steps:
The ammoniacal liquor sweetening agent is supplied with: system comprises storage tank and transferpump.The oxidation of ammoniacal liquor by thionizer bottom is mixed into finite concentration with divider and oxidation air and water coolant and sends into thionizer.Flow by supervisory system control ammoniacal liquor.
Flue gas desulfurization, denitrogenation: flue gas enters thionizer by gas blower by flue system.After flue gas enters thionizer, contact with the whitewashing that comprises the ammoniacal liquor slurries, each jetted layers shower nozzle all is furnished with special-purpose circuitous pump.SO wherein 2Absorb by the ammoniacal liquor slurries, generate ammonium sulphite (NH 4) 2SO 3, surpass 95% SO 2Can be removed.NO in ammonium sulphite and the flue gas 2Reaction generates (NH 4) 2SO 4(ammonium sulfate) and N 2Flue gas passes two the ripple type mist eliminators in thionizer top, removes the drop in the gas.
The oxidation of sulfurous acid ammonia: the absorption tower is furnished with complete oxidation trough and is used for the oxidation ammonium sulphite, and it has enough slurries residence time, guarantees the formation of sufficient oxidation and sulfate of ammoniac xln.Oxidation air is directed onto in the oxidation trough by tubing system and the divider that is installed in the oxidation trough bottom, and the oxidation air system also provides the water coolant of cooling effect and removes SO to the absorption tower simultaneously 2Required ammoniacal liquor.The pH value 6.5~7.0 of slurries in the control absorption tower, this pH value has been optimized SO 2Removal efficient and the oxidation rate of ammonium sulphite.Ammonium sulfate very easily dissolves, and under the thionizer operational conditions, can reach the solubleness of 48% weight, and (in thionizer) ammoniumsulphate soln is in by saturated and contain the ammonium sulfate crystallization body of the suspension of 3~4% weight ratios.The slurries of discharging from thionizer are used to control the concentration of ammonium sulfate crystallization.The ammonium sulfate blowdown pump is delivered to the ammonium sulfate slurries in the device of back one step processing.
5. the processing of desulfuration byproduct sulfate of ammoniac: the treatment facility of ammonium sulfate fertilizer is designed for produces high quality, ready-made available standard level ammonium sulfate fertilizer product.The doctor solution that contains ammonium sulfate generates sulphur ammonium ((NH through evaporative crystallization, dehydration 4) 2SO 4) become dry powder to be collected, deep processing becomes composite chemical fertilizer.
Description of drawings
Fig. 1 is the processing of calcium carbide stove exhaust of the present invention and the process flow sheet that utilizes method again.

Claims (10)

  1. The processing of a calcium carbide stove exhaust with utilize method again, it is characterized in that this method comprises the steps: the preprocessing process of calcium carbide stove exhaust, the tail gas synthetic ammonia process, the absorption of ammonia and course of conveying, ammoniacal liquor flue gas desulfurization, denitrification process, the doctor solution treating processes, wherein
    The preprocessing process of described calcium carbide stove exhaust comprises cooling, dedusting and the scavenging process of calcium carbide stove exhaust;
    Described tail gas synthetic ammonia process adopts the multistage conversion process that CO is transformed into H 2, conversion gas removes CO 2With produce N 2Adopt pressure swing adsorption technique, synthetic ammonia adopts middle-pressure process;
    The absorption of described ammonia and course of conveying are that water absorbs ammonia, make ammoniacal liquor, by pump delivery and be used for boiler flue gas desulfurization, denitrogenation;
    Described ammoniacal liquor flue gas desulfurization, denitrification process are after flue gas advances people's thionizer, contact with the whitewashing that comprises the ammoniacal liquor slurries, generate ammonium sulphite, the NO in ammonium sulphite and the flue gas 2Reaction generates ammonium sulfate and N 2Be oxidized to ammonium sulfate in the oxidation trough of unnecessary subsequently ammonium sulphite in being provided in thionizer, the xln content 3~4% of ammonium sulfate in the control doctor solution;
    The doctor solution treating processes is meant that ammonium sulfate is made for standard compliant chemical fertilizer product after concentrated, crystallization, dehydration.
  2. 2, according to the processing of the described calcium carbide stove exhaust of claim 1 with utilize method again, it is characterized in that: the cooling of described calcium carbide stove exhaust is meant calcium carbide stove exhaust sent in the byproduct steam boiler lowers the temperature.
  3. 3, according to the processing of the described calcium carbide stove exhaust of claim 1 with utilize method again, it is characterized in that: described dust removal process is to realize in the one-level multi-tube dust cleaner.
  4. 4, according to the processing of the described calcium carbide stove exhaust of claim 1 with utilize method again, it is characterized in that: described scavenging process is to adopt washing cooling, caustic wash desulfuration, and the tail gas CO purity after the purification reaches more than 90%.
  5. 5, according to the processing of the described calcium carbide stove exhaust of claim 1 with utilize method again, it is characterized in that: described CO conversion process is realized by 4 sections conversion.
  6. 6, according to the processing of the described calcium carbide stove exhaust of claim 1 with utilize method again, it is characterized in that: described separation of C O 2With produce N 2Adopt molecular sieve transformation suction type.
  7. 7, according to the processing of claim 1 or 5 or 6 described calcium carbide stove exhausts with utilize method again, it is characterized in that: above-mentioned unstripped gas after conversion and decarburization also need be removed CO and CO with the method for methanation behind the first methanolizing 2
  8. 8, according to the processing of the described calcium carbide stove exhaust of claim 1 with utilize method again, it is characterized in that: described synthetic ammonia pressure-controlling is at 30~40MPa.
  9. 9, according to the processing of the described calcium carbide stove exhaust of claim 1 with utilize method again, it is characterized in that: above-mentioned finish the ammonia absorption process after, residual gas is reentered ammonia synthesis converter and is reacted.
  10. 10, according to the processing of the described calcium carbide stove exhaust of claim 1 with utilize method again, it is characterized in that: the doctor solution pH value is controlled at 6.5~7.0 in described ammoniacal liquor flue gas desulfurization, the denitrification process.
CNB200610141746XA 2006-09-30 2006-09-30 Tail gas treatment and reutilization for calcium carbide stove Expired - Fee Related CN100427391C (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CNB200610141746XA CN100427391C (en) 2006-09-30 2006-09-30 Tail gas treatment and reutilization for calcium carbide stove

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CNB200610141746XA CN100427391C (en) 2006-09-30 2006-09-30 Tail gas treatment and reutilization for calcium carbide stove

Publications (2)

Publication Number Publication Date
CN1939840A CN1939840A (en) 2007-04-04
CN100427391C true CN100427391C (en) 2008-10-22

Family

ID=37958419

Family Applications (1)

Application Number Title Priority Date Filing Date
CNB200610141746XA Expired - Fee Related CN100427391C (en) 2006-09-30 2006-09-30 Tail gas treatment and reutilization for calcium carbide stove

Country Status (1)

Country Link
CN (1) CN100427391C (en)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101638359B (en) * 2009-09-04 2011-12-21 傅永茂 Technology for producing oxalic acid by using tail gas of calcium carbide furnace
CN101837954B (en) * 2010-05-18 2012-10-03 浙江工业大学 Method for preparing hydrogen by using tail gas of calcium carbide furnace
CN102745647A (en) * 2012-06-20 2012-10-24 青海宜化化工有限责任公司 Process for producing hydrogen from natural gas by using calcium carbide tail gas
CN103204469B (en) * 2013-03-21 2015-04-08 新疆天业(集团)有限公司 Full-low-transformation technique for tail gas of calcium carbide furnaces
CN103467232B (en) * 2013-08-23 2015-09-02 宁夏宝塔石化科技实业发展有限公司 A kind of method utilizing calcium carbide stove exhaust to prepare alkene
CN104987275B (en) * 2015-07-21 2017-12-08 神雾科技集团股份有限公司 A kind of technique and system of two-part furnace of calcium carbide fine coal ethene
CN105779047A (en) * 2016-04-22 2016-07-20 北京中科瑞奥能源科技股份有限公司 Technology and system for making flue gas into liquified natural gas
CN105838465B (en) * 2016-05-20 2018-07-06 中科瑞奥能源科技股份有限公司 Utilize the technique and system of Fischer-Tropsch process exhaust preparing liquefied natural gas
CN107619055A (en) * 2016-07-17 2018-01-23 卓粤 Tail gas recovery system of calcium carbide furnace
CN106345257B (en) * 2016-08-26 2019-02-26 江苏中圣高科技产业有限公司 A kind of device and method improving ammonia process of desulfurization producing ammonium sulfate byproduct quality
CN107010627B (en) * 2017-04-11 2020-12-25 北京柯林斯达科技发展有限公司 Method for producing pellet calcium carbide raw material by recycling calcium carbide furnace gas fly ash, semi coke powder and quicklime powder

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002126448A (en) * 2000-07-31 2002-05-08 Showa Denko Kk Method and apparatus for treating combustion exhaust gas
CN1394667A (en) * 2002-06-28 2003-02-05 巨化集团公司 Method for treating smoke produced by carbide
CN1456546A (en) * 2003-03-18 2003-11-19 四川亚联高科技有限责任公司 Method for preparing potassium formate and sodium formate from carbide furnace tail gas as raw material
CN1478585A (en) * 2003-07-19 2004-03-03 重庆正和生物能源有限公司 Smoke desucfuration denitrification dedust process and device
CN1600410A (en) * 2003-09-24 2005-03-30 北京国纬达环保科技有限公司 Integration method for ammonia process of desulfurizing flue gas and multiple utilizing desulfurized products and equipment
CN1724369A (en) * 2005-07-20 2006-01-25 赵中彦 Process for producing synthetic ammonia or methanol by acetylene furnace tail gas

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002126448A (en) * 2000-07-31 2002-05-08 Showa Denko Kk Method and apparatus for treating combustion exhaust gas
CN1394667A (en) * 2002-06-28 2003-02-05 巨化集团公司 Method for treating smoke produced by carbide
CN1456546A (en) * 2003-03-18 2003-11-19 四川亚联高科技有限责任公司 Method for preparing potassium formate and sodium formate from carbide furnace tail gas as raw material
CN1478585A (en) * 2003-07-19 2004-03-03 重庆正和生物能源有限公司 Smoke desucfuration denitrification dedust process and device
CN1600410A (en) * 2003-09-24 2005-03-30 北京国纬达环保科技有限公司 Integration method for ammonia process of desulfurizing flue gas and multiple utilizing desulfurized products and equipment
CN1724369A (en) * 2005-07-20 2006-01-25 赵中彦 Process for producing synthetic ammonia or methanol by acetylene furnace tail gas

Also Published As

Publication number Publication date
CN1939840A (en) 2007-04-04

Similar Documents

Publication Publication Date Title
CN100427391C (en) Tail gas treatment and reutilization for calcium carbide stove
CN103303872B (en) System device and method for recycling sulfur dioxide from fume to prepare sulfur
CN106430116B (en) A method of the sulphur-bearing waste solution extracting sulfuric acid generated using coal gas wet oxidation method
CN204727611U (en) The processing unit of sulfuric acid is produced by coke oven gas desulfurization product
CN203507793U (en) Device for simultaneously removing sulfur dioxide and nitrogen oxide from coke oven flue gas
TWI751430B (en) Acid gas treatment
CN205653162U (en) System for sulphuric acid is prepared to sulphur waste liquid that contains that utilizes coal gas wet oxidation process to produce
CN101934191A (en) Method for desulfurizing and denitrating smoke simultaneously through ammonia method
CN103303877A (en) Comprehensive multi-gas source low-concentration SO2 fume recycling acid-making technological process
CN105797562B (en) The double ammonia process integration desulfurization denitration systems of coking flue gas two-part
CN103072957A (en) Technology for preparing sulfuric acid
CN101723334A (en) Raw material pretreatment process for preparing sulfuric acid by using low-quality sulfur and sulphur-bearing waste solution
CN103977682A (en) Simultaneous desulfurization and denitrification method for flue gas
CN102658016A (en) Method for ammonia method desulfurization of flue gas and high-purity ammonium hydrogen sulfite by-producing
CN201658945U (en) Sintering smoke purifying system based on heat pipe afterheat recovery technology
CN110894064A (en) Device and method for preparing sulfuric acid by cracking and regenerating waste sulfuric acid and/or sulfur-containing waste liquid
CN102600710B (en) Treatment method of high-concentration ammonia nitrogen wastewater
CN111514736A (en) Flue gas desulfurization and denitrification system and method combining ozone oxidation with ammonia spraying
CN103100294A (en) Method for removing oxynitride from flue gas through ozone oxidation method
CN113856441B (en) Ammonia desulfurization method and ammonia desulfurization apparatus
CN105381699A (en) Hydrogen peroxide oxidation combined amino wet desulphurization and denitration method and device
US3172725A (en) Production of sulfuric acid
CN101774550B (en) Novel production method of sulfuric acid
CN111495160A (en) Desulfurization and denitrification system and method by using ozone oxidation in cooperation with ammonia process
CN217961993U (en) Ammonia process desulfurization and decarbonization tower and chemicals coproduction device

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
ASS Succession or assignment of patent right

Owner name: YINGLITE ELECTRIC POWER GROUP CO., LTD., NINGXIA;

Free format text: FORMER OWNER: YINGLITE ELECTRIC POWER GROUP CO., LTD., NINGXIA

Effective date: 20080321

C41 Transfer of patent application or patent right or utility model
TA01 Transfer of patent application right

Effective date of registration: 20080321

Address after: 297, east the Great Wall Road, Jinfeng District, the Ningxia Hui Autonomous Region, Yinchuan: 750001

Applicant after: Ningxia British power group Limited by Share Ltd

Co-applicant after: Ningxia Yinglite Chemistry Industry Co., Ltd.

Address before: 297, east the Great Wall Road, Jinfeng District, the Ningxia Hui Autonomous Region, Yinchuan: 750001

Applicant before: Ningxia Yinglite Electric Power Group Co., Ltd.

C14 Grant of patent or utility model
GR01 Patent grant
C17 Cessation of patent right
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20081022

Termination date: 20100930