CN214437776U - Integrated energy-saving environment-friendly ammonia desulfurization crystallization system - Google Patents
Integrated energy-saving environment-friendly ammonia desulfurization crystallization system Download PDFInfo
- Publication number
- CN214437776U CN214437776U CN202022981804.8U CN202022981804U CN214437776U CN 214437776 U CN214437776 U CN 214437776U CN 202022981804 U CN202022981804 U CN 202022981804U CN 214437776 U CN214437776 U CN 214437776U
- Authority
- CN
- China
- Prior art keywords
- absorption
- section
- tower
- tail gas
- quenching
- 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
Images
Classifications
-
- 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
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The utility model relates to an energy-concerving and environment-protective type ammonia process desulfurization crystal system of integral type. The system uses the integrated absorption oxidation crystallization equipment to produce the byproduct ammonium sulfate, and has the advantages of short process flow, low energy consumption, small occupied area and investment saving. Firstly, removing a large amount of moisture carried by tail gas, and processing the tail gas into neutral purified water; absorbing sulfur dioxide in the tail gas by ammonia to generate high-concentration ammonium sulfate slurry; setting a multi-stage ammonia injection facility to control different process concentrations to guarantee the absorption effect and ensure that the tail gas emission meets the requirements of the national standard special emission limit under various working conditions; and the recycled purified water is adopted for cascade washing to realize ultra-clean discharge; the waste heat of the tail gas is recovered to dry the ammonium sulfate and eliminate white smoke, thereby greatly reducing energy consumption and improving the image of a factory; the ammonium sulfate has large particles and low water content. The utility model has the advantages of no evaporation of ammonium sulfate slurry steam, no waste liquid discharge, no fresh water consumption, low energy consumption and less smoke gas amount in the production process; and the equipment is integrated, so that the multifunctional function of one tower is realized, the equipment quantity is small, and the short-process energy-saving and environment-friendly byproduct ammonium sulfate is obtained.
Description
Technical Field
The utility model belongs to the technical field of contain sulphur tail gas processing environmental protection, a system of sulphur recovery unit tail gas treatment and byproduct ammonium sulfate is related to. The method adopts ammonia to absorb sulfur dioxide, and produces ammonium sulfate as a byproduct through integrated absorption oxidation crystallization equipment, so that the process flow is short, the occupied area is small, the investment is low, the energy consumption is low, the tail gas emission of the device meets the requirements of national standard special emission limit, no fresh water is consumed, no waste liquid is discharged, no ammonia escapes, and the ultra-clean emission is realized.
Background
Along with the development of global sulfur-containing crude oil and natural gas resources in a large quantity and the continuous development of coal chemical industry, sulfur recovery has become indispensable supporting environmental protection device, but sulfur recovery unit operating mode is complicated, except normal operating mode, has multiple operating mode: the device is started, prevulcanized, shut down, blown sulfur, passivated, by-pass and other working conditions, and short-term raw material fluctuation during normal production, and the difference of the exhaust gas emission concentration under different working conditions is large. In recent years, with the stricter standards for protecting the atmospheric environment in countries around the world, the emission requirements of sulfur recovery devices are also stricter. At present, most domestic areas require that tail gas of an acid gas treatment device must be subjected to special atmospheric emission limitation, namely the emission concentration of sulfur dioxide is less than 100mg/Nm3And (6) executing. In order to ensure the standard emission of tail gas under various working conditions, the original two-stage Claus and amine method tail gas treatment technology cannot meet the requirement of standard emission of all working conditions.
Therefore, chemical absorption technologies such as ammonia absorption, alkali absorption and the like are applied to the sulfur recovery device in a dispute manner, the tail gas of the sulfur recovery device is ensured to be discharged up to the standard through stable acid-alkali neutralization reaction, but a large amount of wastewater containing ammonia and salt is generated after absorption and needs to be treated again. No matter the wastewater is directly discharged from sewage treatment plants, or is filtered, evaporated and crystallized, the processes of by-producing ammonium sulfate and sodium sulfate can generate wastewater discharge, and secondary pollution is caused.
The desulfurization wastewater has great harm to the environment, and the concrete expression is as follows: (1) the desulfurization wastewater contains high-concentration sulfate and can be reduced into S in water environment2-And then the methyl mercury is generated through relevant reactions, so that the survival of aquatic organisms is influenced, and the original ecological function of the water body is changed; (2) the desulfurization wastewater is weakly acidic, can dissolve heavy metals and certain toxic substances, and can have adverse effects on soil and water environment when being directly discharged, for example, selenium entering soil and water can affect human health, and chronic poisoning can be caused when the selenium is accumulated for a long time.
The common domestic and foreign desulfurization wastewater treatment method comprises the following steps: coagulation-precipitation method, chemical-microfiltration membrane method, biochemical method, evaporative concentration method, artificial wetland method, zero-valent iron method, fluidized bed method, electric drive membrane method, etc. The utility model discloses a dense looks absorption method of low temperature and steam stripping method reduce waste water production and with the whole recovery cleaning of waste water for ammonium sulfate and purified water in the system, the purified water can be used as system make-up water and mill's cooling cycle water station make-up water.
The process of by-producing ammonium sulfate is usually complicated, and a series of processes such as oxidation, evaporation, crystallization, concentration, filtration, drying and the like are required, so that the process is long. And the working procedure is intermittent continuous production, and the equipment is generally operated one by one, so that the equipment has the defects of large number, large occupied area and high investment.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide an energy-saving environment-friendly ammonia desulphurization zero-emission process of a sulfur recovery device with a short flow, which has low energy consumption and by-product ammonium sulfate; the sulfur dioxide emission concentration of the tail gas is less than 20mg/Nm in normal operation3(ii) a And is suitable for the tail gas sulfur dioxide emission concentration of less than 100mg/Nm under the working conditions of device start-up, prevulcanization, shutdown, sulfur blowing, passivation, by-pass and the like and the abnormal conditions of short-term raw material large fluctuation and the like during normal production3No fresh water consumption, no wastewater discharge, no ammonia escape and ultra-clean discharge. Solves the problems of large smoke gas amount, waste water discharge and high energy consumption in the prior art. The main equipment for producing the ammonium sulfate as a byproduct is an all-in-one equipment, and multiple functions of quenching, absorption, oxidation and crystallization are combined, so that the flow is shortened, and the occupied area and the investment are saved. The process route of the utility model is as follows: quenching, absorption, oxidation and crystallization; a guard absorption and washing section; a stripping section; separating, filtering, drying, metering and packaging.
The purpose of the utility model can be realized by the following technical scheme:
an integrated energy-saving environment-friendly ammonia desulfurization crystallization system comprises an integrated quenching absorption tower and a security absorption washing system;
the integrated quenching absorption tower comprises a tail gas quenching section at the top, a two-stage absorption section at the middle part and a solution storage area at the bottom, wherein the solution storage area sequentially comprises a primary oxidation section, a secondary oxidation section, a primary crystallization section and a secondary crystallization section from top to bottom;
the output end of tail gas from the incineration of the sulfur device is connected with the top of the integrated quenching absorption tower through a tail gas heat exchanger, the bottom of the tail gas quenching section is provided with a separation device, and the separated liquid is connected with the upper part of the tail gas quenching section through a quenching water air cooler and a quenching water heat exchanger; the two-stage absorption section in the middle part is respectively one-stage dynamic wave absorption and two-stage reverse spray absorption; the lower primary oxidation section of the integrated quenching absorption tower collects crystallization mother liquor from a mother liquor buffer tank and absorption liquid at the bottom of a security absorption washing system; the primary oxidation section at the lower part of the integrated quenching absorption tower is further divided into an ammonia injection zone and an oxidation zone, the solution in the oxidation zone is provided with two ammonia injection zones, and the liquid in one ammonia injection zone is connected with the primary absorption section at the lower part of the separation device through a dynamic wave circulating pump; liquid in the other ammonia injection area is conveyed to a secondary absorption section at the lower part of the primary absorption section by a spraying circulating pump;
the first-stage oxidation section is connected with the second-stage oxidation section through an overflow pipe or a pump, the first-stage crystallization section is a dilute solid phase region, the second-stage crystallization section is a concentrated solid phase region, and concentrated solid phases after second-stage crystallization are sequentially conveyed to a centrifugal system and an ammonium sulfate treatment system through a concentrated phase conveying pump at the bottom of the tower;
and conveying the tail gas absorbed by the secondary absorption section to a security absorption washing system and then emptying.
The utility model discloses among the technical scheme: the separation device also has an output end which is connected with the upper part of the stripping tower through the purified water heat exchanger, the output end at the top of the stripping tower is connected with the top of the quenching absorption tower, and the output end at the bottom of the stripping tower is connected with the resin exchange deacidification facility through the purified water heat exchanger, the purified water pump and the resin exchange deacidification facility.
The utility model discloses among the technical scheme: air distribution pipes are arranged in the primary oxidation section and the secondary oxidation section, and ammonia distribution pipes are arranged in the ammonia injection area.
The utility model discloses among the technical scheme: the inner diameter of the tower body where the secondary absorption section is located is larger than that of the tower body where the primary absorption section is located, and the tower body where the primary absorption section is located is sleeved in the inner cavity of the tower body where the secondary absorption section is located.
The utility model discloses among the technical scheme: the gas output end of the secondary absorption section is connected with the lower part of the security absorption washing tower, and the security absorption washing tower is sequentially provided with an absorption layer, a water washing layer and a defoaming layer from bottom to top.
The utility model discloses among the technical scheme: the bottom of the security absorption washing tower is provided with a liquid storage area, and the liquid storage area is divided into a plurality of intervals for storing absorption liquid or washing liquid in each area in the tower.
The utility model discloses among the technical scheme: the ammonium sulfate processing system comprises a centrifugal filter and a screw feeder, the screw feeder is connected with an amplitude dryer, one end of the amplitude dryer is connected with a metering packaging system through an ammonium sulfate storage hopper, the other end of the amplitude dryer is connected with a fine powder ammonium sulfate storage hopper through a cyclone separator, and the output end of the top of the cyclone separator is connected with a tail gas washing tower.
An energy-saving and environment-friendly ammonia desulphurization zero-emission method for realizing a sulfur recovery device by using the system comprises the following steps:
(1) waste heat recovery is carried out on fresh air through a tail gas heat exchanger, the temperature is raised to 120-250 ℃, and a part of heated hot air is used as ammonium sulfate of an ammonium sulfate preparation system for drying; the residual gas is used as the smoke supplementary gas of the security absorption washing tower and is used for eliminating white smoke;
tail gas after burning of the sulfur device after heat exchange enters the upper part of the integrated quenching absorption tower and is sprayed by multiple layers of quenching water in a forward or reverse direction, gas and liquid are fully contacted, then the tail gas is separated by a separation device, a separated liquid phase quenching water part is cooled by a quenching water air cooler and a quenching water heat exchanger and returns to the top of the integrated quenching absorption tower for recycling, and the rest part is heated by a purified water heat exchanger and then is sent to the top of the integrated stripping tower for stripping;
the tail gas rapid cooling gas-liquid separation is followed and is continued to the one-level absorption section of integral type rapid cooling absorption tower down, and the power wave band sprays against current or following current with the ammonium sulfate solution of integral type rapid cooling absorption tower bottom, gets into the second grade absorption section after the absorption of one-level absorption section and carries out reverse absorption that sprays:
(2) and conveying the tail gas absorbed by the secondary absorption section to a security absorption washing system for secondary absorption and washing, conveying absorption liquid at the bottom of the security absorption washing tower to the lower part of the integrated quenching absorption tower, pumping the absorption liquid to a secondary oxidation section, a primary crystallization section and a secondary crystallization section after primary oxidation, and then conveying a concentrated solid phase after secondary crystallization to a centrifugal system and an ammonium sulfate treatment system in sequence by a concentrated phase conveying pump at the bottom of the tower.
In some specific embodiments, the process route of the present invention is: quenching, absorption, oxidation and crystallization; a guard absorption and washing section; a stripping section; separating, filtering, drying, metering and packaging.
The detailed scheme is as follows:
1. quenching, absorption, oxidation and crystallization
The part comprises tail gas waste heat recovery and quenching, two-stage absorption, two-stage oxidation and crystallization parts. The main equipment is an integrated quenching absorption tower. The main process is as follows:
recovering waste heat of tail gas: the hot tail gas after burning of the sulfur recovery device is cooled by fresh air heat exchange, and the cooled tail gas after waste heat recovery enters a tail gas quenching part. The hot fresh air after recovering the waste heat can be used as the drying air for drying the crystallized ammonium sulfate; the air can also be used as smoke supplementary gas, and hot air and purified smoke are mixed and heated and then discharged from a chimney for eliminating white smoke from the smoke.
Quenching: the tail gas entering the quenching section is sprayed in a three-stage forward mode, gas and liquid are fully contacted, quenching and cooling are carried out, and most of moisture in the tail gas is condensed by circulating quenching water. After gas-liquid separation, the tail gas continuously descends to a two-stage absorption part; the separated quenching water is pressurized by a pump, most of the separated quenching water is cooled and returned to the top of a quenching section for circulating quenching, and a small part of the separated quenching water is heated and then sent to the top of a stripping tower for stripping.
Two-stage absorption: after the liquid phase is separated by quenching, the tail gas enters a two-stage absorption section, and the absorption of the tail gas is low-temperature absorption, so that the amount of the micro-particle salt mist generated by high-temperature quenching absorption can be greatly reduced. The sulfur dioxide enters a first-stage absorption, namely a power wave band, and is sprayed with the ammonium sulfate solution in a concurrent flow or countercurrent flow manner, so that the sulfur dioxide is efficiently absorbed by adiabatic saturation. After the tail gas is discharged from the power wave, the tail gas enters a secondary absorption section, namely, reverse spray absorption: the dynamic wave outer tower body is locally amplified, and has the functions of spraying, separating and liquid storage, tail gas overflows from the bottom of the dynamic wave to the outer tower body and then moves upwards to the upper part of the outer tower body, dilute ammonium sulfite solution is arranged at a tower outlet for washing, and the tail gas enters a security absorption and washing part after being washed. The upper part of the outer tower body is provided with a facility for spraying circulating liquid at the lower part of the tower, and the countercurrent absorption enhances the absorption effect; the middle part is a gas-liquid separation zone, tail gas goes upward, and spray liquid goes downward; the bottom is the stock solution district, and the subregion sets up annotates ammonia district and oxidation area: absorption liquid with different concentrations can be formed in different areas, ammonia is uniformly distributed in an ammonia injection area by arranging an ammonia injection facility to ensure the absorption capacity of each circulating liquid, and the area of the area is small, so that the absorption capacity of the solution can be rapidly adjusted in case of emergency ammonia injection and the like, and the condition of large system fluctuation can be met; an air distribution pipe is arranged in the oxidation zone and used for ammonium sulfite oxidation, and the area of the zone is large and is primary oxidation. The ammonium sulfate solutions at the bottom are respectively pumped to the inner spray head and the outer spray head of the dynamic wave by a pump to circularly spray so as to carry out the absorption of two stages of solutions with different concentrations; the remaining solution overflows or is pumped to the lower secondary oxidation stage. The inlet of the circulating pump can also be provided with an ammonia injection facility.
Oxidation and crystallization: the lower part of the primary oxidation, namely the lower part of the tower, is provided with a secondary oxidation and crystallization area which is a secondary oxidation section, a primary crystallization section and a secondary crystallization section from top to bottom; the device is connected with the primary oxidation section by an overflow communicating pipe and can also be sent into a secondary oxidation area by a pump, and a partition plate is arranged between the two oxidation areas to divide the two oxidation areas into two areas. The ammonium sulfate circulating liquid after the primary oxidation enters a secondary oxidation section through overflow or pumping, the secondary oxidation section is also provided with an air distribution pipe, and secondary oxidation tail gas is absorbed and washed from the upper part of the section to the lower part of a security absorption tower; the upper part of the oxidation air distribution pipe is a secondary oxidation section, and the lower part of the oxidation air distribution pipe is a two-stage crystallization section. The upper part of the crystallization section is a dilute solid phase region and a primary crystallization section; the lower part is a concentrated solid phase area and a secondary crystallization section. And (4) conveying the concentrated solid phase after the secondary crystallization from the concentrated phase at the bottom of the tower to a subsequent centrifugal separation part by a pump. And (4) after the slurry in the dilute solid phase region is subjected to gravity separation and crystallization, the slurry is sent back to the primary oxidation region by the dilute phase circulating pump to be continuously injected with ammonia, and then sulfur dioxide is circularly absorbed. Compressed air is introduced into the bottommost part of the tower, short blowing is carried out periodically, gas phase stirring is carried out, and material accumulation at the bottom of the tower and blockage of a discharge hole pipeline are prevented. The oxidizing air is provided by an oxidizing blower.
The integrated quenching absorption tower is a multifunctional tower, quenching, absorption, oxidation and crystallization are completed in the tower, and the integrated quenching absorption tower has seven functions of quenching, absorption, separation, oxidation, ammonia injection, crystallization and liquid storage. The top is tail gas quench zone, and the middle part is the two-stage absorption section, and the lower part is two-stage oxidation and two-stage crystallization section, and wherein one-level oxidation section and second grade oxidation section are separated by the baffle, and other all distinguish according to the liquid level.
In the integrated quenching absorption tower, through two-stage absorption, particularly power wave bands, the absorption efficiency is high, the concentration of injected ammonia can be adjusted, the fluctuation resistance is good, and the formation and entrainment of particle salt mist in gas phase are reduced through low-temperature absorption; most of sulfur dioxide in the tail gas is absorbed, and the residual sulfur dioxide enters a security absorption part along with the tail gas.
The first-stage oxidation and the second-stage oxidation at the lower part of the tower are both strong oxidation processes, and the retention time and the total oxidation efficiency are ensured through the two-stage full oxidation.
The two-stage crystallization is static crystallization, has no interference or disturbance, few crystal nuclei, quick crystallization and easy growth of crystals. The two-stage crystallization ensures sufficient retention time, high concentration of ammonium sulfate slurry at the lower part, large crystallization amount, small circulation amount, large crystallization particles, easy sedimentation, easy separation and less ammonium sulfate powder.
2. Security absorption and washing
The part comprises security absorption, water washing, foam removal and emptying. The main equipment is a security absorption washing tower.
Tail gas which is absorbed by the two stages of the integrated quenching absorption tower enters a security absorption area at the lower part of the security absorption washing tower, the tail gas goes up along the tower and is circularly sprayed in a counter-current manner by dilute ammonium sulfite solution at the bottom of the tower to absorb residual sulfur dioxide in the tail gas. The absorption liquid is collected to the absorption liquid area at the bottom of the tower by a liquid collecting disc, most of the absorption liquid is conveyed to the absorption area by an external circulating pump of the tower, and the rest absorption liquid is used as the absorption liquid supplement for quenching absorption. The absorption liquid area is provided with an emergency ammonia injection function, so that the security absorption of the upstream sulfur recovery device when the process control fluctuates greatly is guaranteed.
The flue gas continuously goes up to a water washing area, and is washed by countercurrent spraying of a washing solution corresponding to the bottom of the tower, so that liquid drops and particle salt mist carried in the flue gas are replaced and trapped, the formation of aerosol is reduced, the dust content in the tail gas is reduced, and the ammonia escape is eliminated. The washing liquid is also collected to a tower bottom washing liquid area through a liquid collecting disc and is circularly conveyed to the upper part of the tower by an external tower washing pump.
And after washing, the smoke is subjected to defoaming, mixed with hot air subjected to heat recovery by waste heat of tail gas, heated and discharged from a chimney.
The security guard absorption washing is five-in-one equipment which comprises the following components from bottom to top: liquid storage area, security absorption area, water washing area, defoaming area and chimney. Wherein, divide into a plurality of check in the liquid storage district, supply each district storage absorption liquid or washing liquid in the tower. The absorption area and the washing area can be provided with or without fillers for better absorption and washing effects. One, two or three stage absorption and water washing stages may be provided. If three-stage water washing is adopted, three water washing liquid areas are required to be arranged at the bottom of the tower, the washing liquid overflows and is communicated from top to bottom, and the concentration of dissolved substances is gradually increased.
3. Stripping
The main equipment of the stripping part is a stripping tower and a reboiler, or the stripping tower and the reboiler can be combined into integrated equipment, the sulfur-containing wastewater condensed by quenching is subjected to steam stripping to be regenerated into purified water, and the sulfur-containing tail gas at the tower top is returned to the tail gas quenching part. The purified water is cooled and pumped to deacidification facilities such as resin exchange facilities to be treated into neutral purified water for cooling of a machine pump in the device, water supplement at a washing section and the like, and the redundant purified water is sent to a circulating water station of a factory system to be used as make-up water. Waste acidic water generated by the deacidification facility enters the ammonium sulfate absorption liquid for recycling through washing.
In the stripping tower, all the systems recover waste water for stripping regeneration, sulfur dioxide and carbon dioxide are stripped, and purified water is returned to the systems for recycling after deacidification.
4. Separate filtration, drying and metering packaging
And conveying the concentrated crystallization phase to a centrifugal filter for centrifugal liquid-solid separation. The crystallization mother liquor is recovered to a mother liquor tank and is pumped to the lower part of the quenching absorption tower to supplement the spraying circulating liquid for circulating absorption. The utility model discloses set up two-stage static crystallization, the crystallization dense phase contains the mother liquor volume few, and the mother liquor groove volume can suitably reduce, sparingly invests in and takes up an area of.
And conveying the dehydrated crystal to an amplitude dryer through a screw feeder. And (3) taking hot air obtained after the waste heat of the quenching part is recovered as a heat source, drying by adopting amplitude, feeding dried ammonium sulfate particles into a small buffer hopper, and metering and packaging. And (3) pressurizing the dry tail gas by a fan after the dry tail gas is dedusted by a tail gas cyclone separator, feeding the dry tail gas into a tail gas washing tower, washing the dry tail gas by a first-stage circulating washing liquid, and feeding the tail gas subjected to washing and dedusting to a water washing section of a security absorption washing tower for continuous multi-stage water washing. Fresh water consumption and ammonia escape do not exist, and ultra-clean emission of tail gas is ensured; the concentrated washing liquid is sent back to the bottom of the security absorption tower to be used as a supplementary liquid.
The utility model discloses among the technical scheme: the mass concentration of the crystal in the dilute solid phase region is 1-10%, and the mass concentration of the crystal in the concentrated solid phase region is 5-30%; and the mass concentration of the crystals in the concentrated solid phase is greater than the mass concentration of the crystals in the dilute solid phase region.
The utility model has the advantages that:
firstly: the common domestic and foreign desulfurization wastewater treatment method comprises the following steps: coagulation-precipitation method, chemical-microfiltration membrane method, biochemical method, evaporative concentration method, artificial wetland method, zero-valent iron method, fluidized bed method, electric drive membrane method, etc. The utility model discloses combine concentrated method of evaporation and steam stripping method, add integral type strip facility, with the whole clean processing of retrieving of waste water in the system for ammonium sulfate and purified water, the purified water can regard as system's make-up water and mill's cooling cycle water station make-up water.
Secondly, the utility model relates to a method of zero release energy-concerving and environment-protective type sulphur tail gas treatment to absorb oxidation crystallization equipment by-product ammonium sulfate with integral type rapid cooling, tail gas sulfur dioxide emission concentration is less than 20mg/Nm during normal operation3(ii) a And the tail gas emission of the device meets the requirements of various working conditions of the sulfur recovery device for emission, and under the abnormal conditions of working conditions of the device such as start-up, pre-vulcanization, shutdown, sulfur blowing, passivation, by-pass and the like and short-term raw material large-amplitude fluctuation during normal production, an emergency ammonia injection measure is adopted, the absorption efficiency of the absorption liquid is rapidly improved by utilizing large ammonia injection amount and high circulating concentration, so that the tail gas sulfur dioxide emission concentration is less than 100mg/Nm3(ii) a The waste water after quenching is recycled, and no ammonium sulfate slurry is steamedSteaming, no fresh water consumption and no waste water discharge; and the equipment adopts integration, realizes multiple functions of one tower and produces the ammonium sulfate as a byproduct in a short process. The method has the advantages of wide application range, short flow, small quantity of equipment, low energy consumption, investment and land occupation saving, and solves the problems of large smoke volume, waste water discharge and high energy consumption in the prior art.
Drawings
FIG. 1 is a flow chart of ammonia desulfurization zero-emission process.
In the figure, 1 is an air fan, 2 is a tail gas heat exchanger, 3 is an integrated quenching absorption tower, 4 is a stripping tower, 5 is a dynamic wave circulating pump, 6 is a spray circulating pump, 7 is a dilute phase circulating pump, 8 is a quenching water circulating pump, 9 is a quenching water air cooler, 10 is a quenching water heat exchanger, 11 is a purified water heat exchanger, 12 is a purified water pump, 13 is a deacidification facility, 14 is a security absorption washing tower, 15 is a demister, 16 is a chimney, 17 is an oxidation fan, 18 is a security absorption circulating pump, 19 is a primary water washing pump, 20 is a secondary water washing pump, 21 is a tertiary water washing pump, 22 is a fine powder ammonium sulfate storage hopper, 23 is a dense phase delivery pump, 24 is a centrifugal filter, 25 is a mother liquid tank, 26 is a mother liquid tank pump, 27 is a washing liquid pump, 28 is a tail gas washing tower, 29 is a dry tail gas fan, 30 is a screw feeder, 31 is an amplitude drier, 32 is an ammonium sulfate storage hopper, 33 is a metering package system, 34 is a cyclone separator, and 35 is a stripper reboiler.
Detailed Description
The present invention will be further explained with reference to the following embodiments, but the scope of the present invention is not limited thereto:
referring to fig. 1, an integrated energy-saving environment-friendly ammonia desulfurization crystallization system comprises an integrated quenching absorption tower 3 and a security absorption washing system;
the integrated quenching absorption tower 3 comprises a tail gas quenching section at the top, a two-stage absorption section at the middle part and a solution storage area at the bottom, wherein the solution storage area sequentially comprises a primary oxidation section, a secondary oxidation section, a primary crystallization section and a secondary crystallization section from top to bottom;
the output end of tail gas from the incineration of the sulfur device is connected with the top of an integrated quenching absorption tower 3 through a tail gas heat exchanger 2, the bottom of a tail gas quenching section is provided with a separation device, and separated liquid is connected with the upper part of the tail gas quenching section through a quenching water air cooler 9 and a quenching water heat exchanger 10; two-stage absorption sections in the middle, wherein one stage is dynamic wave absorption, and the second stage is reverse spray absorption; the lower primary oxidation section of the integrated quenching absorption tower 3 collects crystallization mother liquor from a mother liquor buffer tank and absorption liquid at the bottom of a security absorption washing system; the primary oxidation section is also provided with two ammonia injection zones and an oxidation zone, and the liquid in one ammonia injection zone is connected with the primary absorption section at the lower part of the separation device through a dynamic wave circulating pump; liquid in the other ammonia injection area is conveyed to a secondary absorption section at the lower part of the primary absorption section by a spraying circulating pump;
the first-stage oxidation section is connected with the second-stage oxidation section through an overflow pipe or a pump, the first-stage crystallization section is a dilute solid phase region, the second-stage crystallization section is a concentrated solid phase region, and concentrated solid phases after second-stage crystallization are sequentially conveyed to a centrifugal system and an ammonium sulfate treatment system through a concentrated phase conveying pump at the bottom of the tower;
and conveying the tail gas absorbed by the secondary absorption section to a security absorption washing system and then emptying.
The separator also has an output end, the output end is connected with the upper part of the stripping tower 4 through the purified water heat exchanger 11, the output end at the top of the stripping tower 4 is connected with the top of the integrated quenching absorption tower 3, and the output end at the bottom of the stripping tower 4 is connected with the resin exchange deacidification facility 13 through the purified water heat exchanger 11, the purified water pump 12.
Air distribution pipes are arranged in the primary oxidation section and the secondary oxidation section. The ammonia injection area is provided with an ammonia gas distribution pipe.
The inner diameter of the tower body where the secondary absorption section is located is larger than that of the tower body where the primary absorption section is located, and the tower body where the primary absorption section is located is sleeved in the inner cavity of the tower body where the secondary absorption section is located.
The gas output end of the secondary absorption section is connected with the lower part of the security absorption washing tower 14, and the security absorption washing tower 14 is sequentially provided with an absorption layer, a water washing layer and a defoaming layer from bottom to top.
The bottom of the security absorption washing tower 14 is provided with a liquid storage area, and the liquid storage area is divided into a plurality of sections for storing absorption liquid or washing liquid in each section in the tower.
The ammonium sulfate treatment system comprises a centrifugal separator 24 and a screw feeder 30, the screw feeder 30 is connected with an amplitude dryer 31, one end of the amplitude dryer 31 is connected with the metering packaging system through an ammonium sulfate storage hopper 32, the other end of the amplitude dryer 31 is connected with a fine powder ammonium sulfate storage hopper 22 through a cyclone separator 34, and the output end of the top of the cyclone separator 34 is connected with a tail gas washing tower 28.
The detailed implementation mode is as follows:
the process route of the utility model is as follows: quenching, absorption, oxidation and crystallization; a guard absorption and washing section; a stripping section; separating, filtering, drying, metering and packaging. The detailed scheme is as follows:
1. quenching, absorption, oxidation and crystallization
The part comprises tail gas waste heat recovery and quenching, two-stage absorption, two-stage oxidation and crystallization parts. The main equipment is an integrated quenching absorption tower. The main process is as follows:
recovering waste heat of tail gas: after the sulfur recovery device burns, hot tail gas SO at about 300-350 DEG C2The concentration is about 500-30000 mg/Nm3Fresh air is adopted for heat exchange and cooling, and cooled tail gas after waste heat recovery enters a tail gas quenching part at the temperature of 220-300 ℃. The hot fresh air with the waste heat recovered at 120-250 ℃ can be used as drying air for drying the crystallized ammonium sulfate; the air can also be used as smoke supplementary gas, and hot air and purified smoke are mixed and heated to 110-150 ℃ until the smoke is discharged from a chimney, so that the air is used for eliminating white smoke from the smoke.
Quenching: and (3) the tail gas entering the quenching section is subjected to three-stage forward spraying, the gas phase and the liquid phase are fully contacted, the quenching and the temperature reduction are carried out, and 96-98% of most of moisture in the tail gas is condensed by circulating quenching water. After gas-liquid separation, the tail gas continuously descends to a two-stage absorption part; and (3) pressurizing the separated quenching water by a pump, cooling most of the separated quenching water to 30-40 ℃, returning the cooled quenching water to the top of a quenching section for circulating quenching, and heating a small part of the cooled quenching water to 95 ℃ and then delivering the heated quenching water to the top of a stripping tower for stripping.
Two-stage absorption: after the liquid phase is separated by quenching, the tail gas enters a two-stage absorption section, the absorption of the tail gas is low-temperature absorption of 35-50 ℃, and the amount of the micro-particle salt mist generated by high-temperature quenching absorption can be greatly reduced. The sulfur dioxide enters a first-stage absorption, namely a power wave band, and is sprayed with the ammonium sulfate solution in a concurrent flow or countercurrent flow manner, so that the sulfur dioxide is efficiently absorbed by adiabatic saturation. After the tail gas is discharged from the power wave, the tail gas enters a secondary absorption section, namely, reverse spray absorption: the dynamic wave outer tower body is locally amplified, and has the functions of spraying, separating and liquid storage, tail gas overflows from the bottom of the dynamic wave to the outer tower body and then moves upwards to the upper part of the outer tower body, dilute ammonium sulfite solution is arranged at a tower outlet for washing, and the tail gas enters a security absorption and washing part after being washed. The upper part of the outer tower body is provided with a facility for spraying circulating liquid at the lower part of the tower, and the countercurrent absorption enhances the absorption effect; the middle part is a gas-liquid separation zone, tail gas goes upward, and spray liquid goes downward; the bottom is the stock solution district, and the subregion sets up annotates ammonia district and oxidation area: absorption liquid with different concentrations can be formed in different areas, ammonia is uniformly distributed by arranging an ammonia injection facility in an ammonia injection area to ensure the absorption capacity of each circulating liquid, and the area of the area is small, so that the large-flow emergency ammonia injection is facilitated to form high-concentration solution to quickly adjust the solution absorption capacity so as to cope with the condition of large system fluctuation; an air distribution pipe is arranged in the oxidation zone and used for ammonium sulfite oxidation, and the area of the zone is large and is primary oxidation. The ammonium sulfate solutions at the bottom are respectively pumped to the inner spray head and the outer spray head of the dynamic wave by a pump to circularly spray so as to carry out the absorption of two stages of solutions with different concentrations; the remaining solution overflows or is pumped to the lower secondary oxidation stage. The inlet of the circulating pump can also be provided with an ammonia injection facility.
Oxidation and crystallization: the lower part of the primary oxidation, namely the lower part of the tower, is provided with a secondary oxidation and crystallization area which is a secondary oxidation section, a primary crystallization section and a secondary crystallization section from top to bottom; the device is connected with the primary oxidation section by an overflow communicating pipe and can also be sent into a secondary oxidation area by a pump, and a partition plate is arranged between the two oxidation areas to divide the two oxidation areas into two areas. The ammonium sulfate circulating liquid after the primary oxidation enters a secondary oxidation section through overflow or pumping, the secondary oxidation section is provided with an air distribution pipe, and secondary oxidation tail gas enters the lower part of the security absorption tower from the space above the secondary oxidation section for absorption and washing; the upper part of the oxidation air distribution pipe is a secondary oxidation section, and the lower part of the oxidation air distribution pipe is a two-stage crystallization section. The upper part of the crystallization section is a dilute solid phase region and a primary crystallization section; the lower part is a concentrated solid phase area and a secondary crystallization section. And (4) conveying the concentrated solid phase after the secondary crystallization from the concentrated phase at the bottom of the tower to a subsequent centrifugal separation part by a pump. And (4) after the slurry in the dilute solid phase region is subjected to gravity separation and crystallization, the slurry is sent back to the primary oxidation region by the dilute phase circulating pump to be continuously injected with ammonia, and then sulfur dioxide is circularly absorbed. Compressed air is introduced into the bottommost part of the tower, short blowing is carried out periodically, gas phase stirring is carried out, and material accumulation at the bottom of the tower and blockage of a discharge hole pipeline are prevented. The oxidizing air is provided by an oxidizing blower. Wherein: the mass concentration of the crystal in the dilute solid phase region is 1-10%, and the mass concentration of the crystal in the concentrated solid phase region is 5-30%; and the mass concentration of the crystals in the concentrated solid phase is greater than the mass concentration of the crystals in the dilute solid phase region. .
The integrated quenching absorption tower is a multifunctional tower, quenching, absorption, oxidation and crystallization are completed in the tower, and the integrated quenching absorption tower has seven functions of quenching, absorption, separation, oxidation, ammonia injection, crystallization and liquid storage. The top is tail gas quench zone, and the middle part is the two-stage absorption section, and the lower part is two-stage oxidation and two-stage crystallization section, and wherein one-level oxidation section and second grade oxidation section are separated by the baffle, and other all distinguish according to the liquid level.
The ammonia injection device is integrated in a quenching absorption tower, and has the advantages of high absorption efficiency, adjustable ammonia injection concentration and good fluctuation resistance through two-stage absorption, particularly power wave bands, and the formation and entrainment of fine particle salt fog in a gas phase are reduced through low-temperature absorption; most of sulfur dioxide in the tail gas is absorbed, and the residual sulfur dioxide enters a security absorption part along with the tail gas.
The first-stage oxidation and the second-stage oxidation at the lower part of the tower are both strong oxidation processes, and the retention time and the total oxidation efficiency are ensured through the two-stage full oxidation.
The two-stage crystallization is static crystallization, has no interference or disturbance, few crystal nuclei, quick crystallization and easy growth of crystals. The two-stage crystallization ensures sufficient retention time, high concentration of ammonium sulfate slurry at the lower part, large crystallization amount, small circulation amount, large crystallization particles, easy sedimentation, easy separation and less ammonium sulfate powder.
2. Security absorption and washing
The part comprises security absorption, water washing, foam removal and emptying. The main equipment is a security absorption washing tower.
Tail gas which is absorbed by the two stages of the integrated quenching absorption tower enters a security absorption area at the lower part of the security absorption washing tower, the tail gas goes upward along the tower and is circularly sprayed in a counter-current manner by dilute ammonium sulfite solution at the bottom of the tower to absorb residual sulfur dioxide in the tail gas. The absorption liquid is collected to the absorption liquid area at the bottom of the tower by a liquid collecting disc, most of the absorption liquid is conveyed to the absorption area by an external circulating pump of the tower, and the rest absorption liquid is used as the absorption liquid supplement for quenching absorption. The absorption liquid area is provided with an emergency ammonia injection function, so that the security absorption of the upstream sulfur recovery device when the process control fluctuates greatly is guaranteed.
The flue gas continuously goes up to a water washing area, and is washed by countercurrent spraying of a washing solution corresponding to the bottom of the tower, so that liquid drops and particle salt mist carried in the flue gas are replaced and collected, the formation of aerosol is reduced, the dust content in the tail gas is reduced, and the ammonia escape is eliminated. The washing liquid is also collected to a tower bottom washing liquid area through a liquid collecting disc and is circularly conveyed to the upper part of the tower by an external tower washing pump.
And after washing, the smoke is subjected to defoaming, mixed with hot air subjected to heat recovery by waste heat of tail gas, heated and discharged from a chimney.
The security guard absorption washing is five-in-one equipment which comprises the following components from bottom to top: liquid storage area, security absorption area, water washing area, defoaming area and chimney. Wherein, divide into a plurality of check in the liquid storage district, supply each district storage absorption liquid or washing liquid in the tower. The absorption area and the washing area can be provided with or without fillers for better absorption and washing effects. One, two or three stage absorption and water washing stages may be provided. If three-stage water washing is adopted, three water washing liquid areas are required to be arranged at the bottom of the tower, the washing liquid overflows and is communicated from top to bottom, and the concentration of dissolved substances is gradually increased.
3. Stripping
The main equipment of the stripping part is a stripping tower and a reboiler, or the stripping tower and the reboiler can be combined into integrated equipment, the sulfur-containing wastewater condensed by quenching is subjected to steam stripping to be regenerated into purified water, and the sulfur-containing tail gas at the tower top is returned to the tail gas quenching part. The purified water is cooled and pumped to deacidification facilities such as resin exchange facilities to be treated into neutral purified water for cooling of a machine pump in the device, water supplement at a washing section and the like, and the redundant purified water is sent to a circulating water station of a factory system to be used as make-up water. Waste acidic water generated by the deacidification facility enters the ammonium sulfate absorption liquid for recycling through washing.
In the stripping tower, all the systems recover waste water for stripping regeneration, sulfur dioxide and carbon dioxide are stripped, and purified water is returned to the systems for recycling after deacidification.
4. Separate filtration, drying and metering packaging
And conveying the concentrated crystallization phase to a centrifugal filter for centrifugal liquid-solid separation. The crystallization mother liquor is recovered to a mother liquor tank and is pumped to the lower part of the quenching absorption tower to supplement the spraying circulating liquid for circulating absorption. The utility model discloses set up two-stage static crystallization, the crystallization dense phase contains the mother liquor volume few, and the mother liquor groove volume can suitably reduce, sparingly invests in and takes up an area of.
And conveying the dehydrated crystal to an amplitude dryer through a screw feeder. And (3) taking hot air obtained after the waste heat of the quenching part is recovered as a heat source, drying by adopting amplitude, feeding dried ammonium sulfate particles into a small buffer hopper, and metering and packaging. And (3) pressurizing the dry tail gas by a fan after the dry tail gas is dedusted by a tail gas cyclone separator, feeding the dry tail gas into a tail gas washing tower, washing the dry tail gas by a first-stage circulating washing liquid, and feeding the tail gas subjected to washing and dedusting to a water washing section of a security absorption washing tower for continuous multi-stage water washing. Fresh water consumption and ammonia escape do not exist, and ultra-clean emission of tail gas is ensured; the concentrated washing liquid is sent back to the bottom of the security absorption tower to be used as a supplementary liquid.
The utility model provides an integrated energy-saving and environment-friendly ammonia desulphurization system and method for a sulfur recovery device, and uses integrated quenching to absorb low-energy-consumption by-product ammonium sulfate of oxidation crystallization equipment. The sulfur dioxide emission concentration of the tail gas is less than 20mg/Nm in normal operation3(ii) a And the tail gas emission of the device meets the emission of various working conditions of the sulfur recovery device, and the tail gas sulfur dioxide emission concentration is less than 100mg/Nm under the abnormal conditions of working conditions of the device such as start-up, prevulcanization, shutdown, sulfur blowing, passivation, by-pass and the like and short-term raw material large-amplitude fluctuation during normal production3(ii) a The regenerated quenching wastewater is recycled, fresh water is not consumed, and 8-10 t/h purified water can be additionally provided for recycling by taking an 8-ten-thousand-ton/year sulfur device as an example; the mother liquor, the evaporative condensate and the washing liquid of the ammonium sulfate treatment part return to the absorption part for recycling, and no waste water is discharged; wide application range and SO treatment2The concentration range is about 500-30000 mg/Nm3(ii) a The equipment is integrated to realize one-tower multifunctional integrated quenching absorption tower, seven functions of quenching, two-stage absorption, separation, oxidation, ammonia injection, crystallization and liquid storage are integrated, and the security absorption tower integrates absorption, two-stage washing, defoaming and chimney into a whole, thereby effectively realizing the functions of quenching, two-stage absorption, separation, oxidation, ammonia injection, crystallization and liquid storageTen devices and pipelines are reduced, and the occupied area is saved by about 100m2The investment is reduced by about 200 ten thousand yuan; the tail gas heat source is effectively utilized, and the energy consumption is reduced by 1900 kW; effectively solves the problems of large smoke volume, waste water discharge and high energy consumption in the prior art.
Claims (7)
1. The utility model provides an energy-concerving and environment-protective type ammonia process desulfurization crystal system of integral type which characterized in that: the system comprises an integrated quenching absorption tower (3) and a security absorption washing system;
the integrated quenching absorption tower (3) comprises a tail gas quenching section at the top, a two-stage absorption section at the middle part and a solution storage area at the bottom, wherein the solution storage area sequentially comprises a primary oxidation section, a secondary oxidation section, a primary crystallization section and a secondary crystallization section from top to bottom;
the output end of tail gas from the incineration of the sulfur device is connected with the top of the integrated quenching absorption tower (3) through a tail gas heat exchanger (2), the bottom of the tail gas quenching section is provided with a separation device, and the separated liquid is connected with the upper part of the tail gas quenching section through a quenching water air cooler (9) and a quenching water heat exchanger (10); the two-stage absorption section in the middle part is a first-stage dynamic wave absorption section and a second-stage reverse spraying absorption section respectively; the lower primary oxidation section of the integrated quenching absorption tower (3) collects crystallization mother liquor from a mother liquor buffer tank and absorption liquid at the bottom of a security absorption washing system; the primary oxidation section at the lower part of the quenching absorption tower (3) is also provided with an oxidation zone and two ammonia injection zones, and the liquid in one ammonia injection zone is connected with the primary absorption section at the lower part of the separation device through a dynamic wave circulating pump; liquid in the other ammonia injection area is conveyed to a secondary absorption section at the lower part of the primary absorption section by a spraying circulating pump;
the first-stage oxidation section is connected with the second-stage oxidation section through an overflow pipe or a pump, the first-stage crystallization section is a dilute solid phase region, the second-stage crystallization section is a concentrated solid phase region, and concentrated solid phases after second-stage crystallization are sequentially conveyed to a centrifugal system and an ammonium sulfate treatment system through a concentrated phase conveying pump at the bottom of the tower;
and conveying the tail gas absorbed by the secondary absorption section to a security absorption washing system and then emptying.
2. The integrated energy-saving environment-friendly ammonia desulphurization crystallization system according to claim 1, characterized in that: the separation device also has an output end which is connected with the upper part of the stripping tower (4) through the purified water heat exchanger (11), the output end at the top of the stripping tower (4) is connected with the top of the quenching absorption tower (3), and the output end at the bottom of the stripping tower (4) is connected with the resin exchange deacidification facility (13) through the purified water heat exchanger (11), the purified water pump (12).
3. The integrated energy-saving environment-friendly ammonia desulphurization crystallization system according to claim 1, characterized in that: air distribution pipes are arranged in the primary oxidation section and the secondary oxidation section, and ammonia distribution pipes are arranged in the ammonia injection area.
4. The integrated energy-saving environment-friendly ammonia desulphurization crystallization system according to claim 1, characterized in that: the inner diameter of the tower body where the secondary absorption section is located is larger than that of the tower body where the primary absorption section is located, and the tower body where the primary absorption section is located is sleeved in the inner cavity of the tower body where the secondary absorption section is located.
5. The integrated energy-saving environment-friendly ammonia desulphurization crystallization system according to claim 1, characterized in that: the gas output end of the secondary absorption section is connected with the lower part of the security absorption washing tower (14), and the security absorption washing tower (14) is sequentially provided with an absorption layer, a water washing layer and a defoaming layer from bottom to top.
6. The integrated energy-saving environment-friendly ammonia desulphurization crystallization system according to claim 5, characterized in that: the bottom of the security absorption washing tower (14) is provided with a liquid storage area, and the liquid storage area is divided into a plurality of sections for storing absorption liquid or washing liquid in each section in the tower.
7. The integrated energy-saving environment-friendly ammonia desulphurization crystallization system according to claim 1, characterized in that: the ammonium sulfate processing system comprises a centrifugal filter (24) and a screw feeder (30), the screw feeder (30) is connected with an amplitude dryer (31), one end of the amplitude dryer (31) is connected with a metering and packaging system through an ammonium sulfate storage hopper (32), the other end of the amplitude dryer is connected with a fine powder ammonium sulfate storage hopper (22) through a cyclone separator (34), and the output end of the top of the cyclone separator (34) is connected with a tail gas washing tower (28).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022981804.8U CN214437776U (en) | 2020-12-11 | 2020-12-11 | Integrated energy-saving environment-friendly ammonia desulfurization crystallization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022981804.8U CN214437776U (en) | 2020-12-11 | 2020-12-11 | Integrated energy-saving environment-friendly ammonia desulfurization crystallization system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214437776U true CN214437776U (en) | 2021-10-22 |
Family
ID=78188488
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022981804.8U Active CN214437776U (en) | 2020-12-11 | 2020-12-11 | Integrated energy-saving environment-friendly ammonia desulfurization crystallization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214437776U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112717652A (en) * | 2020-12-11 | 2021-04-30 | 中石化南京工程有限公司 | Integrated energy-saving environment-friendly ammonia desulphurization crystallization system and method |
-
2020
- 2020-12-11 CN CN202022981804.8U patent/CN214437776U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112717652A (en) * | 2020-12-11 | 2021-04-30 | 中石化南京工程有限公司 | Integrated energy-saving environment-friendly ammonia desulphurization crystallization system and method |
| CN112717652B (en) * | 2020-12-11 | 2022-10-14 | 中石化南京工程有限公司 | Integrated energy-saving environment-friendly ammonia desulphurization crystallization system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2018040852A1 (en) | System and method for treating desulfurization wastewater using flue gas waste heat | |
| CN101579602B (en) | Energy-saving and high-quality ammonia desulphurization process for ammonia sulfate recovery | |
| EP2990096B1 (en) | Method and apparatus for treating acidic tail gas by using ammonia process | |
| CN106430116B (en) | A method of the sulphur-bearing waste solution extracting sulfuric acid generated using coal gas wet oxidation method | |
| CN102228777B (en) | Double-oxidation ammonia desulfurization process and device | |
| CN102160960A (en) | Soda wet desulphurization process and system for sintering flue gas | |
| CN201135851Y (en) | A system for removing the carbon dioxide in flue gas of the generating plant using ammonia process | |
| CN104474850B (en) | Molten sulfur pond exhaust gas treating method and device | |
| CN206652387U (en) | A kind of ammonia desulfuration equipment of resourcebility | |
| CN101433798B (en) | High-efficient wet-type ammonia recovering method desulfuration method with oxidation and concentration processes outside tower and device thereof | |
| CN111841272A (en) | Water-saving and energy-saving ammonia desulphurization emission process and system for preventing ammonia escape aerosol | |
| CN105457479B (en) | A kind of flue gas desulfurization zero-emission resource processing system and method | |
| CN103961996A (en) | Fume purification system with tower box | |
| CN110282606B (en) | Wet processing system and process for aqueous sulfur paste and desulfurization waste liquid | |
| US8795405B1 (en) | Beneficial use of carbon | |
| CN214437776U (en) | Integrated energy-saving environment-friendly ammonia desulfurization crystallization system | |
| CN112717652B (en) | Integrated energy-saving environment-friendly ammonia desulphurization crystallization system and method | |
| CN103861426B (en) | A kind of flue gas desulfurization and dedusting also reclaims the method for sodium sulfite | |
| CN202161911U (en) | Flue gas treatment equipment | |
| CN214437829U (en) | Energy-saving environment-friendly ammonia desulphurization zero-emission system of sulfur recovery device | |
| CN112717653B (en) | Energy-saving environment-friendly ammonia desulphurization zero-emission system and method for sulfur recovery device | |
| CN205517223U (en) | Flue gas desulfurization zero release money source processing system | |
| CN107388847A (en) | Heat reclaim unit and technique in flue gas desulfurization and denitration technique | |
| CN102698582A (en) | Ammonium bicarbonate desulfurization process and ammonium bicarbonate desulfurization process system | |
| CN201676635U (en) | Desulfurizing technology system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |