CN116062710A - System for preparing acid by sulfur foam biphase method and preparation method thereof - Google Patents
System for preparing acid by sulfur foam biphase method and preparation method thereof Download PDFInfo
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
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- 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
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Abstract
The invention provides a sulfur foam biphase acid preparation system and a preparation method thereof. The system for preparing the acid by the sulfur foam biphase method sequentially comprises a pretreatment unit, an incineration unit, a purification unit, a drying unit, a conversion unit, an absorption unit and a tail absorption unit. Adding a pretreatment process before the incineration process, separating ammonium salt and sulfur paste better through pretreatment, concentrating the ammonium salt to reduce the water content, feeding the ammonium salt and the sulfur paste into an incinerator, supplying reaction heat discharged by a combustion reaction, and reducing the consumption of coal gas and the yield of byproduct dilute acid without using coke oven gas for combustion heat compensation; the use can solve the problems of small sulfur simple substance particles, high moisture and more ammonium salts in the sulfur foam, solves the difficult problem of bad treatment of the sulfur foam and desulfurization waste liquid, and has wide application prospect.
Description
Technical Field
The invention relates to the technical field of industrial acid production, in particular to a sulfur foam biphase acid production system and a preparation method thereof.
Background
The coking industry is an important part of the coal industry, and the product coke can be used as fuel for blast furnace smelting and can also be used for casting, nonferrous metal smelting and water gas production; can be used for manufacturing producer gas for producing synthetic ammonia and also can be used for manufacturing calcium carbide to obtain raw materials of the organic synthesis industry. Raw gas at the outlet of the coke oven is purified and washed in a series to obtain clean coke oven gas, sulfur foam and desulfurization waste liquid are generated in the ammonia desulfurization process of the gas, and the clean coke oven gas not only contains sulfur, but also contains ammonium salt and water, and is a mixture. Sulfur foam and desulfurization waste liquid are always headache problems in coking production, and the problem needs to be solved. The sulfur foam is generally melted and solidified into blocky sulfur for sale, and the sulfur has low purity, about 60 percent of sulfur content and more impurities, and is hardly accepted by the market.
At present, the domestic coking industry desulfurization waste liquid acid making process is distinguished from the feeding state and the combustion form, mainly comprises three types of sulfur foam slurry feeding, oxygen-enriched combustion, liquid sulfur and concentrated solution independent feeding, air combustion, sulfur foam dry powder feeding and air combustion, which are respectively and simply called wet acid making, semi-dry acid making and dry acid making. The raw material of the wet process acid preparation is mainly desulfurization waste liquid and sulfur foam.
While the wet method acid preparation can treat desulfurization waste liquid and sulfur foam, on one hand, the desulfurization waste liquid enters an incinerator to be slurry, contains a large amount of water, and needs to consume a large amount of gas during combustion; on the other hand, a large amount of byproduct dilute acid generated in the acid preparation working section cannot be utilized, so that a large amount of environmental pollution and resource waste are caused. How to better utilize the desulfurization waste liquid and the sulfur foam is a difficult problem to be solved.
Disclosure of Invention
The invention aims to: the invention aims to provide a system for preparing acid by a sulfur foam biphase method and a preparation method thereof, which overcome the problems of small sulfur simple substance particles, high water content and more ammonium salts in sulfur foam, better use desulfurization waste liquid and sulfur foam generated by gas desulfurization in coking industry for producing concentrated sulfuric acid, and solve the difficult problem of bad treatment of the sulfur foam and desulfurization waste liquid; and the by-product dilute sulfuric acid generated by using desulfurization waste liquid and sulfur foam as raw materials is correspondingly reduced, the energy loss is reduced, and the yield is improved.
The technical scheme of the invention is as follows:
on one hand, the invention provides a system for preparing acid by a sulfur foam biphase method, which is formed by sequentially connecting a pretreatment unit, an incineration unit, a purification unit, a drying unit, a conversion unit, an absorption unit and a tail absorption unit.
The pretreatment unit comprises a super centrifuge, a sulfur paste slurry storage tank, a sulfur paste slurry pump, a double-phase tower, a sulfur storage tank and a sulfur submerged pump which are connected in sequence.
The incineration unit comprises an incinerator and a waste heat boiler which are sequentially connected.
The purifying unit comprises a dynamic wave scrubber, a packed tower scrubber and a primary and secondary electric demister which are connected in sequence.
The drying unit comprises a drying tower and a drying acid circulation tank.
The conversion unit comprises a sulfur dioxide blower, a first heat exchanger, a three-section catalyst bed, a second heat exchanger and a fourth catalyst bed which are sequentially connected.
The absorption unit comprises a first absorption tower and a second absorption tower which are connected in sequence.
The tail suction unit comprises a tail gas dynamic wave scrubber, a tail gas packing tower scrubber and a tail gas electric-catching demister which are connected in sequence.
The pretreatment unit further comprises a concentration tower, a concentration kettle and a concentrated salt slurry tank which are connected in sequence; the double-phase tower is also communicated with the concentration tower, and the concentrated salt slurry tank is sent into the incinerator through a concentrated salt pump.
In some embodiments, a filter is also provided between the dual phase tower and the sulfur storage tank, which is connected to the incinerator by a submerged pump of sulfur.
In some embodiments, the concentration tower is further provided with a cooling device, the gas enters the cooling device through the demister, and the cooling device is connected with the ejector and then leads to the vacuum water tank; the cooling device can be a primary cooling device and a secondary cooling device which are connected in sequence; the concentrating kettle is also provided with a cooler communicated with the ejector.
In some embodiments, the dual phase column, the concentrating column and the concentrating tank are each provided with a gas line to the incinerator; an air preheater and an electric heater can also be arranged on the gas pipeline.
In some embodiments, the dynamic wave scrubber and the packed tower scrubber are both provided with a circulating scrubbing pump, the outlet of the packed tower scrubber is sequentially connected with a primary electric demister and a secondary electric demister, and the outlet of the secondary electric demister is communicated to the drying process.
In some embodiments, the three-stage catalyst bed is connected to the first absorber tower, the fourth catalyst bed is connected to the second absorber tower, and an electric heater is arranged before the three-stage catalyst bed and the fourth catalyst bed.
In some embodiments, the gas outlet of the second absorber is in turn connected to a tail suction unit.
In another aspect, the invention also provides a preparation method of the sulfur foam biphase method acid, which specifically comprises the following operations by using the system for preparing the sulfur foam biphase acid:
(1) Pretreatment process
Delivering the sulfur foam and the desulfurization waste liquid to a super centrifuge for solid-liquid separation, delivering filtrate to a filtrate tank, pressurizing and returning to a desulfurization system, delivering separated sulfur paste into a sulfur paste storage tank, pressurizing and delivering to a two-phase tower to obtain liquid sulfur and clear liquid; delivering the liquid sulfur into a sulfur storage tank, and entering an incineration procedure; and sending the clear liquid into a concentration tower, concentrating to obtain concentrated salt slurry, sending the concentrated salt slurry into a concentrated salt slurry tank, and concentrating to obtain ammonia water for other process devices.
(2) Incineration process
The liquid sulfur and the concentrated salt slurry sent by the pretreatment process are respectively sent to a liquid sulfur spray gun and a waste liquid spray gun, heated compressed air is respectively atomized, and the burning temperature is controlled by the air quantity of a double-phase feeding quantity burning fan at the temperature of 1100-1150 ℃ to convert sulfur elements of auxiliary salt in the liquid sulfur and the concentrated solution into SO 2 And a small amount of SO 3 The method comprises the steps of carrying out a first treatment on the surface of the High temperature SO from incinerator 2 The furnace gas enters a waste heat boiler for SO 2 Recycling high-temperature waste heat in the process gas to generate saturated steam of 3.5-3.7 MPa; the saturated steam generated is decompressed to 0.7MPa and then sent to a low-pressure steam pipe network for pretreatment;
the desalted water from the external pipe network is fed into a waste heat boiler after chemical adding and deoxidization treatment, and SO coming out of the waste heat boiler is discharged 2 And (3) reducing the temperature of the process gas to 270-300 ℃ and then removing the purification process.
(3) Purification process
SO at 270-300 ℃ from waste heat boiler 2 The process gas sequentially passes through a dynamic wave scrubber, a packed tower scrubber and a two-stage electric demister, and is humidified and cooled by dilute sulfuric acid which is a byproduct of the process gas and cooled by gas, so that a large amount of water, dust, acid mist and the like contained in the process gas are removed, and harmful impurities in the catalyst in the subsequent conversion process are removed. And (3) reducing the temperature of the process gas from the electric demister to 30-35 ℃, and then entering a drying process.
(4) Drying process
SO from the purification step 2 The process gas enters a drying tower to remove water, and the water content of the process gas discharged from the drying tower is less than or equal to 0.1g/Nm 3 Then go through SO 2 The air is pressurized and then sent to a conversion process.
(5) Conversion procedure
SO from the drying step 2 The process gas is firstly passed through SO 2 The blower is pressurized. Enters an I heat exchanger, exchanges heat with high-temperature converted gas to 420 ℃, and enters SO 2 The third section of catalyst bed of the converter enters a fourth catalyst bed for secondary conversion after heat exchange, and then enters a second absorption tower of the absorption procedure after heat exchange and temperature reduction; SO in the process gas under the action of catalyst 2 With O 2 Reacted, catalyzed and oxidized to SO 3 The conversion rate can reach 99.8 percent.
(6) Absorption process
The process gas after primary conversion enters a first absorption tower from the bottom of the tower at 160-170 ℃ to be in countercurrent contact with the absorption acid sprayed from the top of the tower, SO that SO in the process gas is removed 3 And then, returning the defogging product to a conversion system for secondary conversion after defogging by a fiber defogger at the top of the tower.
The process gas after the secondary conversion enters a second absorption tower from the bottom of the tower at 160-170 ℃ to be in countercurrent contact with the absorption acid sprayed from the top of the tower, SO that SO in the process gas is removed 3 Then, the waste water is sent to a tail suction process after demisting by a fiber demister at the top of the tower.
The first and second absorption columns are packed columns. The concentration of sprayed acid in the absorption tower is 98%, SO that SO is absorbed and converted 3 The concentration after the reaction is 98.3%, and the reaction automatically flows to an absorption acid circulating pump tank from the bottom of the tower. 94% of dry acid is serially connected into the tank of the absorption acid circulating pump, the concentration of the absorption acid is maintained to be 98%, and then the absorption acid is pressurized by the absorption tower circulating pump and then is sent to the absorption tower cooler for cooling, and the absorption tower cooler is sent to the absorption tower for circulating spraying for use after cooling. And (3) adding one part of the redundant 98% sulfuric acid into a sulfuric acid buffer tank of a drying tower, and adding the other part of the redundant 98% sulfuric acid serving as finished acid into a finished acid intermediate tank after passing through a cooler.
Before the engineering is started, 50-60 t of 98% concentrated sulfuric acid is needed for pickling passivation, drying and dehumidification, and the concentrated sulfuric acid is provided by an owner and sent to an acid making unit from an oil depot unit. The concentrated sulfuric acid after the acid washing passivation contains a small amount of daub, and needs to be sent to an ammonium sulfate unit for slow consumption.
(7) Tail suction process
The acid making tail gas from the absorption tower enters a tail gas dynamic wave scrubber, and the dilute ammonia water obtained in the pretreatment procedure is used for spraying and absorbing the residual SO in the tail gas 2 Forming ammonium bisulfide and ammonium sulfite solution, and returning the solution to the concentration tower for secondary concentration; the ammonia-containing tail gas from the tail absorption dynamic wave scrubber enters a tail gas filler tower scrubber, volatile ammonia entrained in the tail gas is sprayed by dilute acid from a purification procedure, and the tail gas from the tail gas filler tower scrubber is discharged after acid mist is removed.
In some embodiments, the temperature in the dual-phase tower is 120-140 ℃, the bottom pressure is 0.42-0.5 MPa, and the top pressure is 0.3-0.35 MPa.
In some embodiments, the sulfur reservoir temperature is 135-140 ℃ and the filter inlet-outlet pressure is 0-0.3 mpa.
In some embodiments, the pressure in the concentration tower is-0.07 to-0.09 MPa, and the temperature in the concentration tower is 75-85 ℃.
In some embodiments, the pressure in the concentrating kettle is minus 0.08 to minus 0.09MPa, and the temperature in the kettle is 80-90 ℃.
In some embodiments, the concentrated tank is discharged to a concentrated salt slurry tank when the concentrated tank concentrated salt slurry density reaches 1300 kg/m; the temperature in the concentrated salt slurry tank is 80-85 ℃.
The beneficial effects are that:
the invention provides a sulfur foam biphase acid preparation system and a preparation method thereof. According to the invention, a pretreatment process is added before a common wet acid preparation process, ammonium salt and sulfur paste are better separated through pretreatment, the ammonium salt is concentrated to reduce the water content, the ammonium salt and the sulfur paste enter an incinerator, the reaction heat released by a combustion reaction is supplied, the coke oven gas is not required to be used for combustion and heat compensation, and the use amount of coal and the yield of byproduct dilute acid are reduced; the salt content of ammonia water obtained by concentrating ammonium salt is less than 0.05%, and the ammonia water can be returned to coking chemical process or other working procedures for use, so as to solve the problems of water balance and reasonable utilization of water resources; the system and the method provided by the invention can overcome the problems of small sulfur simple substance particles, high moisture and more ammonium salts in sulfur foam, solve the difficult problem of bad treatment of sulfur foam and desulfurization waste liquid, reduce the emission of byproducts and pollution, and have wide application prospects.
Drawings
FIG. 1 is a schematic diagram showing the flow from pretreatment to drying in the acid making process of the present invention;
fig. 2 is a schematic flow chart of a drying to tail-sucking process in the acid making process of the invention.
Detailed Description
The invention will be described below in connection with specific embodiments. The following examples are illustrative of the present invention and are not intended to limit the present invention. Other combinations and various modifications within the spirit of the invention may be made without departing from the spirit or scope of the invention.
The chemical reagents used in the invention are all common commercial analytical pure unless specified.
Example 1
As shown in fig. 1 and 2, the sulfur foam is derived from coking chemical desulfurization process, and the main component of the sulfur foam is NH 4 CNS、（NH 4 ） 2 S 2 O 3 And the like and a small amount of sulfur.
The sulfur foam 100 cubic meters sent from the desulfurization unit is centrifuged by a super centrifuge, sulfur paste slurry is sent into a sulfur paste slurry storage tank, then the sulfur paste slurry is sent to a double-phase tower through a sulfur paste slurry pump to be heated to 130 ℃, bubbles of the sulfur paste slurry are broken when the double-phase tower is heated, sulfur particles begin to gather and become heavy and sink, the sulfur particles are separated from solution under the action of temperature and pressure, the lower sulfur particles are continuously heated and melted to form liquid sulfur, the liquid sulfur is separated and stored at the bottom of the double-phase tower, the liquid sulfur is sent into a sulfur filter through the self 0.5MPa pressure of the bottom of the tower to be filtered, impurities are removed and then enter the sulfur storage tank, a steam heating coil is arranged in the sulfur storage tank, the temperature is kept at 135-140 ℃, so that the fluidity of the liquid sulfur is guaranteed, and the liquid sulfur is pressurized by a sulfur submerged pump and then sent to a sulfur spray gun of an incinerator to be atomized and burned.
The high Wen Qingye at the top of the double-phase tower enters the concentrating tower through the pressure of 0.35MPa of the high Wen Qingye to be concentrated and evaporated in vacuum, the negative pressure in the tower is kept at-0.07 to-0.09 MPa in the concentrating process, the temperature is controlled to be 75-85 ℃, part of the concentrated solution is conveyed to the concentrating tower through a concentrating circulating pump to circulate, the other part of the concentrated solution is concentrated until the density reaches 1250kg/m, the concentrated solution is sent to a concentrating kettle to be concentrated for the second time, the negative pressure of the concentrating kettle is controlled to be-0.08 to-0.09 MPa, the temperature is controlled to be 80-90 ℃, when the density of the concentrated salt slurry in the concentrating kettle reaches 1300kg/m, the concentrated salt slurry tank is discharged to a concentrated salt slurry tank, the temperature is kept at 80-85 ℃ through steam tracing, and the concentrated salt slurry is pressurized by the pump and then sent to an incinerator waste liquid spray gun to be atomized and then burned.
The ammonia gas evaporated from the concentration tower is subjected to impurity removal through a demister, and after being cooled to 40-45 ℃ through a primary cooler, the cooled ammonia water is returned to the desulfurization system for water supplementing so as to ensure the water balance of the desulfurization system. The uncooled ammonia gas enters a secondary cooler to be continuously cooled to 30-35 ℃, and the obtained ammonia water reaching the standard enters a vacuum water tank through an ejector; on the other hand, ammonia gas evaporated from the concentration kettle is cooled to 30-35 ℃ by a cooler, and ammonia water reaching the standard is obtained and enters a vacuum water tank by an ejector; the ammonia water obtained by the two parts has the salt content less than 0.05 percent and higher quality through detection, can enter the regeneration treatment in the coking chemical process or other processes for use, can solve the water balance problem in the process, and reasonably utilizes water resources to reduce the cost consumption.
The double-phase tower, the concentration tower and the concentration kettle are also provided with gas pipelines, gas which is not concentrated in the evaporation process is collected, and the gas is heated by the air preheater and then is led into the incinerator for incineration, so that all the gas is ensured to be utilized.
The liquid sulfur and the concentrated salt slurry obtained in the pretreatment process are respectively sent to a liquid sulfur spray gun and a waste liquid spray gun, heated compressed air is respectively atomized, and the burning temperature is controlled by the biphase feeding quantity and the air quantity of a combustion fan at the temperature of 1100-1150 ℃ to convert sulfur elements of auxiliary salt in the liquid sulfur and the concentrated solution into SO 2 And a small amount of SO 3 。
In the incineration step, the main chemical incineration and decomposition reactions occurring in the incinerator are as follows:
S+O 2 →SO 2
NH 4 SCN+3O 2 →N 2 +CO 2 +SO 2 +2H 2 O
(NH 4 ) 2 S 2 O 3 +5/2O 2 →N 2 +2SO 2 +4 H 2 O
(NH 4 ) 2 SO 4 +O 2 →N 2 +SO 2 +4 H 2 O
(NH 4 ) 2 CO 3 +3/2O 2 →N 2 +CO 2 +4 H 2 O
4NH 3 +3O 2 →2N 2 +6 H 2 O
SO 2 +O 2 →SO 3
the heat required by the combustion of the incinerator is supplied by the reaction heat released by the combustion reaction, and the coke oven gas is not required to be used for carrying out combustion heat compensation.
High temperature SO from incinerator 2 Process gas enters a waste heat boiler for SO 2 And recycling high-temperature waste heat in the process gas to generate saturated steam of 3.5-3.7 MPa. SO (SO) 2 The process gas is subjected to heat exchange and temperature reduction to 270-300 ℃, then sequentially passes through a dynamic wave scrubber, a packed tower scrubber and a two-stage electric demister, and is humidified and cooled and gas cooled respectively by dilute sulfuric acid which is a byproduct of the process gas, so that a large amount of harmful impurities in catalysts of the subsequent conversion process, such as water, dust, acid mist and the like, contained in the process gas are removed.
The process gas in the reverse jet pipe of the dynamic wave scrubber is in countercurrent contact with dilute sulfuric acid, and enters a packed tower scrubber for cooling and washing after adiabatic humidification and dust removal. Part of the washing acid of the dynamic wave washer enters a reverse spray pipe of the dynamic wave washer to be sprayed for recycling, and the other part of the washing acid is sent to an absorption tower to be used as water supplement.
The packed tower scrubber is mainly used for cooling and scrubbing the process gas. The process gas which is discharged from the dynamic wave scrubber enters from the lower part of the packing tower, and is in countercurrent contact with sprayed circulating dilute acid in the packing layer for heat exchange, the temperature is reduced to 35-40 ℃, the process gas enters into two electric demisters which are operated in series, acid mist and dust carried in the process gas are trapped, and a small amount of dilute acid discharged from the bottom of the electric demister automatically flows to the dynamic wave scrubber.
Considering sudden power failure, residual high-temperature process gas in the system can shorten the service life of glass fiber reinforced plastic equipment and even damage the glass fiber reinforced plastic equipment, so that a high-level tank and an emergency spray head are arranged above the power wave scrubber, the emergency spraying time is 10-20 min, and downstream glass fiber reinforced plastic equipment and pipelines are protected. Meanwhile, in order to prevent the glass fiber reinforced plastic equipment and the pipeline from being imbibed, a safe water seal is arranged on the outlet pipeline of the electric demister.
And (3) reducing the temperature of the process gas from the electric demister to 30-35 ℃, and then entering a drying process.
SO at 30-35 DEG C 2 The process gas enters a drying tower to remove water, the drying tower is a packed tower, and a fiber demister is arranged at the top of the drying tower. The inside of the tower is circularly sprayed with 94% sulfuric acid, the concentration of the sprayed acid after water absorption dilution is 93-93.5%, and the sprayed acid flows into a dry acid circulation tank from the bottom of the tower. The drying acid circulation tank is strung into 98% sulfuric acid at the outlet of the absorption acid cooler to maintain the concentration of the drying circulating acid. And then the cooled circulating acid is sent to a drying tower for circulating spraying. SO exiting the drying tower 2 The moisture content of the process gas is less than or equal to 0.1g/Nm 3 Then go through SO 2 The mixture is pressurized by a blower and sent to a conversion process.
Dried SO 2 The process gas firstly enters the I-th heat exchanger, enters a three-section catalyst bed after heat exchange, and SO in the process gas under the action of the catalyst 2 With O 2 Reaction, catalyzed oxygenConversion to SO 3 . The high-temperature conversion gas coming out of the I-stage catalyst bed passes through an I-th heat exchanger and low-temperature SO 2 After the heat exchange and the temperature reduction of the process gas, the process gas enters a section II catalyst bed for continuous conversion, then enters a section III catalyst bed after the heat exchange and the temperature reduction of a section II heat exchanger, SO as to finish SO 2 The final catalytic oxidation process of the primary conversion stage is finally carried out by a third heat exchanger and is carried out by a third heat exchanger 2 Low temperature SO of blower 2 And after the heat exchange and the temperature reduction of the process gas, removing the process gas from the first absorption tower in the absorption process. Low temperature SO from the first absorber 2 The process gas enters SO after heat exchange by a heat exchanger II 2 A fourth catalyst bed for SO 2 And then the second conversion of the waste water is carried out, and the waste water is removed from the second absorption tower in the absorption process after heat exchange and temperature reduction. The SO 2 The catalytic conversion reaction is as follows:
SO 2 （g）+ ½O 2 （g）→ SO 3 （g）+ 100.32 kj /mol
the process gas after primary conversion enters a first absorption tower from the bottom of the tower at 160-170 ℃ to be in countercurrent contact with the absorption acid sprayed from the top of the tower, SO that SO in the process gas is removed 3 And then, returning the defogging product to a conversion system for secondary conversion after defogging by a fiber defogger at the top of the tower.
The process gas after the secondary conversion enters a second absorption tower from the bottom of the tower at 160-170 ℃ to be in countercurrent contact with the absorption acid sprayed from the top of the tower, SO that SO in the process gas is removed 3 Then, the waste water is sent to a tail suction process after demisting by a fiber demister at the top of the tower.
The 98% concentrated sulfuric acid obtained by absorption flows from the bottom of the tower to an absorption acid circulating pump tank, and is used as finished acid to be sent into a finished acid intermediate tank after passing through a cooler.
The acid making tail gas from the absorption tower sequentially enters a tail gas dynamic wave washer, a tail gas filler tower washer and a tail gas electric-catching demister, ammonia water is used for washing residual sulfur dioxide of the tail gas to form ammonium bisulfide and ammonium sulfite solution, and the ammonium bisulfide and ammonium sulfite solution are returned to the concentration tower for secondary concentration; the tail gas is discharged after treatment, and the treated tail gas meets the standard of GB16171-2012 of emission standard of pollutants in coking chemistry industry.
The present invention is capable of other and further embodiments and its several details are capable of modification and variation in light of the present invention, as will be apparent to those skilled in the art, without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (9)
1. A system for biphasic acid making with sulfur foam, comprising:
the device comprises a pretreatment unit, an incineration unit, a purification unit, a drying unit, a conversion unit, an absorption unit and a tail absorption unit which are sequentially connected;
the pretreatment unit comprises a super centrifuge, a sulfur paste storage tank, a double-phase tower and a sulfur storage tank which are connected in sequence;
the incineration unit comprises an incinerator and a waste heat boiler which are sequentially connected;
the purifying unit comprises a dynamic wave scrubber, a packed tower scrubber and an electric demister which are connected in sequence;
the drying unit comprises a drying tower;
the conversion unit comprises a first heat exchanger, a three-section catalyst bed, a second heat exchanger and a fourth catalyst bed which are sequentially connected;
the absorption unit comprises a first absorption tower and a second absorption tower which are connected in sequence;
the tail suction unit comprises a tail gas dynamic wave scrubber, a tail gas packing tower scrubber and a tail gas electric capturing demister which are connected in sequence;
the pretreatment unit further comprises a concentration tower, a concentration kettle and a concentrated salt slurry tank which are connected in sequence; the double-phase tower is also communicated with the concentration tower, and the concentrated salt slurry tank is communicated to the incinerator.
2. The system for biphasic acid production with sulfur foam according to claim 1, wherein a filter is further provided between the biphasic tower and the sulfur storage tank, and the sulfur storage tank is connected to the incinerator by a submerged pump.
3. The system for preparing acid by the sulfur foam biphase method according to claim 1, wherein the concentration tower is further provided with a cooling device which is connected with the ejector and then led to the vacuum water tank; the concentrating kettle is also provided with a cooler communicated with the ejector.
4. The system for preparing acid by the sulfur foam biphasic method according to claim 1, wherein the biphasic tower, the concentration tower and the concentration kettle are further provided with gas phase pipelines to an incinerator.
5. A method for preparing concentrated sulfuric acid by using the sulfur foam biphase acid preparation system as claimed in any one of claims 1 to 4, which is characterized by comprising the following steps:
(1) Pretreatment procedure: delivering the sulfur foam and the desulfurization waste liquid to a super centrifuge for solid-liquid separation, delivering filtrate to a filtrate tank for pressurized return desulfurization, delivering separated sulfur paste slurry to a sulfur paste slurry storage tank, and delivering the sulfur paste slurry to a double-phase tower for pressurized delivery to obtain liquid sulfur and clear liquid; delivering the liquid sulfur into a sulfur storage tank, and entering an incineration procedure; sending the clear liquid into a concentration tower, concentrating to obtain concentrated salt slurry, sending the concentrated salt slurry into a concentrated salt slurry tank, and concentrating to obtain ammonia water for other process devices;
(2) And (3) incineration procedure: the liquid sulfur and the concentrated salt slurry sent by the pretreatment process are respectively atomized and then burned; high temperature SO from incinerator 2 After the furnace gas enters the waste heat boiler for heat removal, the furnace gas enters a dynamic wave scrubber of the purification unit;
(3) And (3) a purification procedure: SO from waste heat boiler 2 The process gas is humidified, cooled and primarily washed and purified by a dynamic wave scrubber, wet process gas at a dynamic wave outlet enters a packing washing tower to be in countercurrent contact with cooling circulating dilute acid sprayed on the top of the tower, washed and purified, impurities in the process gas are removed, the process gas enters a two-stage electric demister to remove acid mist, and the purified process gas is sent to a drying process;
(4) And (3) a drying procedure: SO from the purification step 2 The process gas is showered with 94% sulfuric acid in a drying tower to remove water, so that the water in the process gas is 0.1g/Nm 3 The mixture is then sent to a conversion step;
(5) Conversion process: SO from the drying step 2 Process gas channel addingAfter pressure and heat exchange, the waste gas enters SO 2 The catalyst bed is subjected to primary and secondary conversion, and then is subjected to heat exchange and temperature reduction, and then is subjected to absorption by an absorption procedure;
(6) Absorption process: SO after the first conversion 2 The process gas is in countercurrent contact with the absorption acid in the first absorption tower, and the demisted process gas returns to the conversion process for secondary conversion; SO after secondary conversion 2 The process gas is in countercurrent contact with the absorption acid in a second absorption tower, defogging is carried out, and then the process gas is sent to a tail absorption process;
(7) Tail suction procedure: the tail gas from the absorption tower sequentially enters a tail gas dynamic wave scrubber, a tail gas filler tower scrubber and a tail gas electric-catching demister, and is discharged after reaching the standard.
6. The method for preparing the sulfur foam biphasic acid according to claim 5, wherein the temperature in the biphasic tower is 120-140 ℃, the bottom pressure is 0.42-0.5 MPa, and the top pressure is 0.3-0.35 MPa.
7. The method for producing an acid by a sulfur foam biphasic method according to claim 5, wherein the temperature of the sulfur storage tank is 135-140 ℃, and the inlet-outlet pressure of the filter is 0-0.3 mpa.
8. The method for preparing the sulfur foam biphasic acid according to the claim 5, which is characterized in that the pressure in the concentration tower is-0.07 to-0.09 MPa, and the temperature in the concentration tower is 75-85 ℃; the pressure in the concentrating kettle is minus 0.08 to minus 0.09MPa, and the temperature in the concentrating kettle is 80-90 ℃.
9. The method for preparing the sulfur foam biphase acid according to claim 5, wherein when the density of the concentrated salt slurry in the concentration kettle reaches 1300kg/m, the concentrated salt slurry is discharged into a concentrated salt slurry tank; the temperature in the concentrated salt slurry tank is 80-85 ℃.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116675184A (en) * | 2023-07-28 | 2023-09-01 | 潍坊春源化工有限公司 | Process and equipment for circularly producing sulfur trioxide |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111285335A (en) * | 2020-02-22 | 2020-06-16 | 江苏康茂环保工程有限公司 | System for preparing sulfuric acid by using sulfur foam and desulfurization waste liquid semidry method and acid preparation method |
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| CN111285335A (en) * | 2020-02-22 | 2020-06-16 | 江苏康茂环保工程有限公司 | System for preparing sulfuric acid by using sulfur foam and desulfurization waste liquid semidry method and acid preparation method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116675184A (en) * | 2023-07-28 | 2023-09-01 | 潍坊春源化工有限公司 | Process and equipment for circularly producing sulfur trioxide |
| CN116675184B (en) * | 2023-07-28 | 2023-11-14 | 潍坊春源化工有限公司 | Process and equipment for circularly producing sulfur trioxide |
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