CN106698362B - A kind of energy-efficient sulfur recovery unit and method - Google Patents
A kind of energy-efficient sulfur recovery unit and method Download PDFInfo
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- CN106698362B CN106698362B CN201710120066.8A CN201710120066A CN106698362B CN 106698362 B CN106698362 B CN 106698362B CN 201710120066 A CN201710120066 A CN 201710120066A CN 106698362 B CN106698362 B CN 106698362B
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
- F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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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
- 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
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Abstract
The present invention provides a kind of energy-efficient sulfur recovery units and method.Sulfur recovery unit provided by the invention includes thermal response system, claus reaction system and tail gas burning and flue gas heat recovery system；Its process mainly comprises the steps that thermal response and claus reaction production sulphur and sulphur tail gas processed, and by-product middle pressure steam occur for acid gas；Sulphur tail gas processed is sent into tail gas burning furnace and is burned；The high-temperature flue gas that tail gas burning furnace generates recycles thermal energy through smoke convection room, i.e., five sections of heat transfer zones, including superheat section, boiler feedwater preheating section, tail gas preheating section, unstripped gas preheating section and sulphur air preheat section processed is arranged in smoke convection room.The waste heat of tail gas burning furnace exiting flue gas can be not only made full use of using sulfur recovery unit and method of the invention, and acid gas, sulphur tail gas processed, sulphur air preheat processed to higher temperature can be made, improve burner for producing sulfur temperature, be conducive to improve sulphur conversion ratio in furnace, fuel gas consumption needed for reducing incinerator.
Description
Technical field
The present invention relates to chemical technology fields, and in particular to be a kind of energy-efficient sulfur recovery unit and method, especially
It is a kind of to burn heat recovery technical optimization using claus process and tail gas and combine the energy-efficient sulphur recovery to be formed
Device and technique.
Background technique
Petrochemical industry is the industry of an opposite highly energy-consuming, energy-saving to have become that be related to petroleum chemical enterprise even whole
The big factors of a industry development.National departments concerned has formulated a series of energy-saving and emission-reduction policy at present, determines that future builds up
Index is advanced, meets the energy conservation standard system of national conditions, main highly energy-consuming trade realization energy consumption limit standard all standing, and 80% or more
Energy efficiency indexes reach advanced world standards.Waste heat, residual temperature comprehensive utilization are improved energetically, are to realize that energy-efficient one is important
Approach.
Sulfur recovery unit is typically provided with tail gas burning furnace, for that will contain a small amount of H in sulphur tail gas processed2S, COS (carbonyl
Sulphur), the harmful substances such as Sx directly burn and are converted into SO2, remaining H2, the substance combustions such as CO and hydro carbons are at H2O and CO2, high temperature cigarette
Gas is directly arranged atmosphere or is sent to downstream process and continues with after heat exchange equipment recycles heat.The H as contained by sulphur tail gas processed2S、
H2, the combustible contents too low (usually less than 3%) such as CO and cannot burn, therefore must be heated to sufficiently high temperature can just make this
A little substances generate corresponding conversion.The fuel that usual incinerator needs is provided by the external fuel gas of device, and fuel gas and air are through pacifying
It is mixed and burned loaded on the burner on incinerator, discharges heat in incinerator combustion chamber, generate high-temperature flue gas, provide in sulphur tail gas processed
The energy that a small amount of combustible conversion reaction needs.
Sulfur recovery unit belongs to the device of heat surplus, how to make good use of device heat, and the mutual Proper Match of heat is made to be
Energy-saving key.Currently, the tail gas burning furnace of sulfur recovery unit, the temperature that combustion chamber generates high-temperature flue gas is generally
650-815 DEG C, which is generally passed through air or generates steam by waste heat boiler to recycle heat, drops flue-gas temperature
It being discharged into atmosphere by chimney after to 300 DEG C or so or is sent to downstream treatment process and carry out deep desulfuration, heat utilization mode is single,
Fume afterheat is underutilized.The sulphur tail gas processed of the tail gas burning furnace entrance of existing claus sulphur recovery units is (general
Be 122-130 DEG C) and air all without being directly entered tail gas burning furnace by preheating, consumed fuel tolerance is larger, operation
It is costly.On the other hand, conventional fume afterheat for generating outer defeated low pressure or middle pressure steam, steam by general full factory's low pressure or middle pressure
Vapour concentrates by-product by boiler, and quantity of steam is more rich, while for fuel gas, and coal steams more economical rationality, therefore,
Sulfur recovery unit does not need outer defeated excessive low pressure or middle pressure steam.In addition, sulfur recovery unit convention acidic unstripped gas and sulphur processed are empty
Gas preheating mainly has the external middle pressure steam of device or the self-produced middle pressure steam two ways of device, both preheating methods are in addition to increasing
Outside equipment investment and operating cost, preheating temperature is also limited through the steam pressure frequently as heat source, that is, uses the steaming of 4.1MPa
Vapour, also only about 240 DEG C of preheating temperature.
Summary of the invention
The purpose of the present invention is to provide a kind of energy-efficient sulfur recovery units and method.Use sulfur recovery of the invention
Device and method can not only make full use of the waste heat of tail gas burning furnace exiting flue gas, and can make acid gas, sulphur tail gas processed, system
Sulphur air preheat can effectively improve burner for producing sulfur temperature to higher temperature, keep operation more stable, be conducive to improve
Sulphur conversion ratio in furnace, and fuel gas consumption needed for incinerator can be reduced.
In order to achieve the above objectives, present invention firstly provides a kind of energy-efficient sulfur recovery units comprising: thermal response
System, claus reaction system and tail gas burn and flue gas heat recovery system；
Wherein, the thermal response system includes: burner for producing sulfur and waste heat boiler；
The tail gas burns and flue gas heat recovery system includes: that tail gas burning furnace is connected to be formed with smoke convection room
Furnace body；The smoke convection room is provided with five sections of heat transfer zones, comprising: superheat section, boiler feedwater preheating section, tail gas preheating section, original
Expect gas preheating section and sulphur air preheat section processed；
Burner for producing sulfur in the thermal response system is connected to waste heat boiler, and the Process Gas outlet of the waste heat boiler is logical
It crosses pipeline and is connected to the claus reaction system；
The steam input pipe line of middle pressure the saturated vapor outlet and the superheat section of the smoke convection room of the waste heat boiler
It is connected, so that the flue gas that the middle pressure saturated vapor of waste heat boiler by-product is generated with the tail gas burning furnace exchanges heat, and will
It is pressed through in after heat exchange defeated outside hot steam；
The boiler feedwater efferent duct of the boiler feedwater preheating section of the admission port of the waste heat boiler and the smoke convection room
Line is connected, so that the medium-pressure boiler water supply from battery limit (BL) exchanges heat with the flue gas after superheat section exchanges heat, and makes to preheat
Medium-pressure boiler water supply afterwards enters waste heat boiler；
The tail gas of the sulphur offgas outlet processed and the tail gas preheating section of the smoke convection room of the claus reaction system is defeated
The one end for entering pipeline is connected, and the other end of the tail gas intake pipeline is connected to the tail gas burning furnace, so that sulphur tail gas processed
With by boiler feedwater preheating section heat exchange after flue gas exchange heat, and make preheating after sulphur tail gas processed enter tail gas burning furnace into
Row burns；
The acidity of the acid gas entrance of the burner for producing sulfur and the unstripped gas preheating section of the smoke convection room is former
Expect the connection of gas intake pipeline, so that acid gas exchanges heat with the flue gas after the heat exchange of tail gas preheating section, and makes to preheat
Acid gas afterwards enters burner for producing sulfur；
The air outlet conduits of the sulphur air preheat section processed of the air intake of the burner for producing sulfur and the smoke convection room
Line is connected, so that air exchanges heat with the flue gas after the heat exchange of unstripped gas preheating section, and makes the sulphur air processed after preheating
Into burner for producing sulfur；
The tail gas burning furnace is additionally provided with a fuel gas entrance and an air intake.
Specific embodiment according to the present invention, it is preferable that the energy-efficient sulfur recovery unit further includes at least one
Platform air blower, the air blower are connected with the air inlet line of the sulphur air preheat section processed of the smoke convection room, and being used for will
The sulphur air preheat section processed of air delivery to smoke convection room exchanges heat with the flue gas after the heat exchange of unstripped gas preheating section, and
Air after making preheating enters burner for producing sulfur.
Specific embodiment according to the present invention, it is preferable that the energy-efficient sulfur recovery unit further includes at least one
Air-introduced machine and at least a chimney, the chimney and the air-introduced machine pass sequentially through the cigarette that pipeline is connected to the smoke convection room
Gas outlet, for by the flue gas (flue gas i.e. after heat is recycled in five sections of heat transfer zones) after sulphur air preheat section processed heat exchange
Send out battery limit (BL).
In above-mentioned energy-efficient sulfur recovery unit, it is preferable that the claus reaction system includes: to pass sequentially through pipe
Second level claus reaction device, three-level claus reaction device and the selective catalytic oxidation reactor of line connection.
In above-mentioned energy-efficient sulfur recovery unit, it is preferable that the tail gas burning furnace is connected with smoke convection room
The furnace body of formation is that vertical incinerator is connected to be formed with horizontal smoke convection roomShape furnace body.
In above-mentioned energy-efficient sulfur recovery unit, it is preferable that the tail gas burning furnace is connected with smoke convection room
The furnace body of formation be vertical incinerator withShape smoke convection room, which is connected, to be formedShape furnace body.
In above-mentioned energy-efficient sulfur recovery unit, it is preferable that the tail gas burning furnace is connected with smoke convection room
The furnace body of formation is that horizontal incinerator and horizontal smoke convection room are coaxially connected the furnace body to be formed.
In above-mentioned energy-efficient sulfur recovery unit, it is preferable that the tail gas burning furnace is vertical and cylindrical incinerator.
In above-mentioned energy-efficient sulfur recovery unit, it is preferable that the tail gas burning furnace is vertical type square incinerator.
In above-mentioned energy-efficient sulfur recovery unit, it is preferable that the tail gas burning furnace is horizontal cylindrical shape incinerator.
In energy-efficient sulfur recovery unit of the invention, burner for producing sulfur, waste heat boiler, second level claus reaction
The specific structure of the components such as device, three-level claus reaction device, selective catalytic oxidation reactor all can be this field it is conventional,
It is not repeating herein.
On the other hand, it the present invention also provides a kind of energy-efficient sulfur recovery method, uses above-mentioned energy-efficient
Sulfur recovery unit, method includes the following steps:
(1) make acid gas and sulphur air processed enter burner for producing sulfur to burn, combustion product enters waste heat boiler
Saturated vapor is pressed in by-product, then waste heat boiler outlet Process Gas enter claus reaction system, after reaction generate sulphur and
Sulphur tail gas processed；
(2) the middle pressure saturated vapor of by-product is made to enter the superheat section of smoke convection room, the flue gas generated with tail gas burning furnace
It exchanges heat, and defeated outside hot steam by pressing through in after heat exchange；
(3) so that the medium-pressure boiler water supply from battery limit (BL) is entered the boiler feedwater preheating section of smoke convection room, overheated with passing through
Flue gas after Duan Huanre exchanges heat, and the boiler feedwater after preheating is made to enter waste heat boiler；
(4) sulphur tail gas processed is made to enter the tail gas preheating section of smoke convection room, with by boiler feedwater preheating section heat exchange after
Flue gas exchanges heat, and so that the sulphur tail gas processed after preheating is entered tail gas burning furnace, while being passed through fuel gas into tail gas burning furnace
And air, to be burned to sulphur tail gas processed；
(5) acid gas is made to enter the unstripped gas preheating section of smoke convection room, with by tail gas preheating section heat exchange after
Flue gas exchanges heat, and so that the acid gas after preheating is entered burner for producing sulfur and burn；
(6) the sulphur air preheat section processed for admitting air into smoke convection room, with the cigarette after the heat exchange of unstripped gas preheating section
Gas exchanges heat, and the air after preheating is made to enter burner for producing sulfur for combustion acid unstripped gas；
(7) by the flue gas (flue gas i.e. after heat is recycled in five sections of heat transfer zones) after sulphur air preheat section processed heat exchange
Send out battery limit (BL).
In above-mentioned energy-efficient sulfur recovery method, it is preferable that the pressure of the middle pressure steam of waste heat boiler by-product is 3.5
~4.4MPaG.
In above-mentioned energy-efficient sulfur recovery method, it is preferable that tail gas burning furnace generate flue-gas temperature be 800~
900 DEG C, after the heat exchange of the middle pressure steam of superheat section and waste heat boiler by-product, obtained middle pressure superheat steam temperature is 420~450
DEG C, the flue-gas temperature after superheat section exchanges heat is 650~700 DEG C.
In above-mentioned energy-efficient sulfur recovery method, it is preferable that the temperature of the medium-pressure boiler water supply from battery limit (BL) is 104
DEG C~132 DEG C, after boiler feedwater preheating section is exchanged heat with 650~700 DEG C of flue gases after superheat section exchanges heat, obtain
Boiler feed temperature after preheating is 240~260 DEG C, and the flue-gas temperature after the heat exchange of boiler feedwater preheating section is 460~500
℃。
In above-mentioned energy-efficient sulfur recovery method, it is preferable that the temperature of sulphur tail gas processed is 122~130 DEG C, in tail gas
Sulphur processed after preheating section is exchanged heat with 460~500 DEG C of flue gases after the heat exchange of boiler feedwater preheating section, after obtained preheating
Exhaust temperature is 250~300 DEG C, and the flue-gas temperature after the heat exchange of tail gas preheating section is 350~400 DEG C.
In above-mentioned energy-efficient sulfur recovery method, it is preferable that into the temperature of the acid gas of unstripped gas preheating section
Degree is 20~40 DEG C, after unstripped gas preheating section is exchanged heat with 350~400 DEG C of flue gases after the heat exchange of tail gas preheating section,
Acid gas temperature after obtained preheating is 250~300 DEG C, and the flue-gas temperature after the heat exchange of unstripped gas preheating section is
260~320 DEG C.
In above-mentioned energy-efficient sulfur recovery method, it is preferable that the temperature of air for entering sulphur air preheat section processed is
Room temperature obtains after sulphur air preheat section processed is exchanged heat with 260~320 DEG C of flue gases after the heat exchange of unstripped gas preheating section
Preheating after air themperature be 250~300 DEG C, by sulphur air preheat section processed heat exchange after flue-gas temperature be 180~240
℃。
In energy-efficient sulfur recovery method of the invention, burner for producing sulfur, waste heat boiler, second level claus reaction
It the design parameter of reaction conducted in the components such as device, three-level claus reaction device, selective catalytic oxidation reactor and adopts
Catalyst etc. all can be this field it is conventional, repeat no more herein.
In energy-efficient sulfur recovery unit and method of the invention, it should be noted that, in the present invention that just brings into operation
Device when, into burner for producing sulfur acid gas and air be the acid gas and air not exchanged heat, to
Device operation a period of time after generating sulphur tail gas and high-temperature flue gas processed, recycles flue gas to acid gas, sulphur air processed and system
Sulphur tail gas etc. exchanges heat, and acid gas, the sulphur air processed after heat exchange are sent into burner for producing sulfur.
Energy-efficient sulfur recovery unit provided by the invention mainly include thermal response system, claus reaction system and
Tail gas burns and flue gas heat recovery system；Energy-efficient sulfur recovery method provided by the invention mainly comprises the steps that
Thermal response and claus reaction production sulphur and sulphur tail gas processed, and by-product middle pressure steam occur for acid gas；Sulphur tail gas processed is sent
The tail gas burning furnace entered in tail gas burning and flue gas heat recovery system is burned；The high-temperature flue gas warp that tail gas burning furnace generates
Thermal energy is recycled in smoke convection room in tail gas burning and flue gas heat recovery system, i.e., five sections of heat exchange is arranged in smoke convection room
Area mainly includes superheat section, boiler feedwater preheating section, tail gas preheating section, unstripped gas preheating section and sulphur air preheat section processed.
Compared with prior art, the invention has the following advantages that
(1) for the first time by acid gas, sulphur air processed, the sulphur tail gas material processed preheating collection in Crouse's recovery technology of sulfur
At in the smoke convection room after tail gas burning furnace, the different potential temperature heats of flue gas are rationally utilized, fume afterheat obtains abundant benefit
With.
(2) device efficiency is high, and process flow is simple, and equipment investment is low, and land occupation saves, and process flow is short, technical process safety
Reliably, the biggish technique of risk or equipment is not present.
(3) tail gas burning furnace not byproduct steam is supplied to the logistics for needing to heat using this part of waste heat, has saved device
Fuel gas consumption.
In conclusion can not only make full use of tail gas burning furnace exiting flue gas using sulfur recovery unit and method of the invention
Waste heat, and acid gas, sulphur tail gas processed, sulphur air preheat processed to higher temperature can be made；Effectively improve sulphur combustion processed
The temperature for burning furnace keeps operation more stable, is conducive to improve sulphur conversion ratio in furnace, and significantly reduce needed for incinerator
Fuel gas consumption；Overcome existing burning outlet of still high-temperature flue gas heat do not make full use of or byproduct steam caused by fuel
Waste and the acid gas limitation low with sulphur air preheating temperature processed；And then can save the energy, reduce operating cost,
Equipment investment is reduced, shortens process flow, improve device efficiency.
Detailed description of the invention
Fig. 1 is the energy-efficient sulfur recovery unit structure and process flow diagram that embodiment 1 provides；
Fig. 2 is the energy-efficient sulfur recovery unit structure and process flow diagram that embodiment 2 provides；
Fig. 3 is the energy-efficient sulfur recovery unit structure and process flow diagram that embodiment 3 provides；
Primary clustering symbol description:
1- burner for producing sulfur；2- waste heat boiler；3- second level claus reaction device；4- three-level claus reaction device；5- selection
Property catalyst oxidation reactor；6- tail gas burning furnace；7- smoke convection room；8- superheat section；9- boiler feedwater preheating section；10- tail gas
Preheating section；11- unstripped gas preheating section；12- sulphur air preheat section；13- air blower；14- air-introduced machine；15- chimney.
Specific embodiment
In order to which technical characteristic of the invention, purpose and beneficial effect are more clearly understood, now in conjunction in detail below
Embodiment and Figure of description carry out following detailed description to technical solution of the present invention, but should not be understood as can to of the invention
The restriction of practical range.
Embodiment 1
Present embodiments provide a kind of energy-efficient sulfur recovery unit, as shown in Figure 1, comprising: thermal response system, gram
Louth reaction system, tail gas burns and flue gas heat recovery system, air blower 13, air-introduced machine 14 and chimney 15；
Wherein, the thermal response system includes: burner for producing sulfur 1 and waste heat boiler 2；
The claus reaction system includes: second level claus reaction device 3, three-level claus reaction device 4 and selectivity
Catalyst oxidation reactor 5；
The tail gas burns and flue gas heat recovery system includes: that tail gas burning furnace 6 is connected to be formed with smoke convection room 7
Furnace body, which is that vertical incinerator is connected with horizontal smoke convection room to be formedShape furnace body, the vertical burning
Furnace is vertical and cylindrical incinerator；The smoke convection room 7 is provided with five sections of heat transfer zones, comprising: superheat section 8, boiler feedwater are pre-
Hot arc 9, tail gas preheating section 10, unstripped gas preheating section 11 and sulphur air preheat section 12 processed；
Burner for producing sulfur 1 in the thermal response system is connected to waste heat boiler 2, and the Process Gas of the waste heat boiler 2 goes out
Mouthful by pipeline be sequentially connected to second level claus reaction device 3, the three-level claus reaction device 4 of the claus reaction system with
And selective catalytic oxidation reactor 5；
The steam input pipe of middle pressure the saturated vapor outlet and the superheat section 8 of the smoke convection room 7 of the waste heat boiler 2
Line is connected, so that the flue gas that the middle pressure saturated vapor of 2 by-product of waste heat boiler is generated with the tail gas burning furnace 6 exchanges heat,
And it is defeated outside hot steam by pressing through in after heat exchange；
The boiler feedwater of the boiler feedwater preheating section 9 of the admission port of the waste heat boiler 2 and the smoke convection room 7 exports
Pipeline is connected, so that the medium-pressure boiler water supply from battery limit (BL) exchanges heat with the flue gas after the heat exchange of superheat section 8, and makes pre-
Boiler feedwater after heat enters waste heat boiler 2；
The tail gas of the tail gas preheating section 10 of the sulphur offgas outlet processed and smoke convection room 7 of the claus reaction system
One end of intake pipeline is connected, and the other end of the tail gas intake pipeline is connected to the tail gas burning furnace 6, so that sulphur tail processed
Gas exchanges heat with the flue gas after the heat exchange of boiler feedwater preheating section 9, and the sulphur tail gas processed after preheating is made to enter tail gas burning
Furnace 6 is burned；
The acid of the acid gas entrance of the burner for producing sulfur 1 and the unstripped gas preheating section 11 of the smoke convection room 7
Property unstripped gas intake pipeline connection so that acid gas with by tail gas preheating section 10 exchange heat after flue gas exchange heat, and
Acid gas after making preheating enters burner for producing sulfur 1；
The air intake of the burner for producing sulfur 1 and the air of the sulphur air preheat section 12 processed of the smoke convection room 7 are defeated
Pipeline is connected out, so that sulphur air processed exchanges heat with the flue gas after the heat exchange of unstripped gas preheating section 11, and after making preheating
Air enter burner for producing sulfur 1；
The chimney 15 passes sequentially through the exhanst gas outlet that pipeline is connected to the smoke convection room 7 with the air-introduced machine 14,
For that will be sent out by the flue gas (flue gas i.e. after heat is recycled in five sections of heat transfer zones) after sulphur air preheat section 12 processed heat exchange
Battery limit (BL)；
The tail gas burning furnace 6 is additionally provided with a fuel gas entrance and an air intake.
The present embodiment additionally provides a kind of energy-efficient sulfur recovery method, uses above-mentioned device, as shown in Figure 1,
For producing sulphur amount and be 20,000 tons/year, method includes the following steps:
(1) make acid gas enter burner for producing sulfur 1 with air to burn, subsequently into 2 by-product 3.5 of waste heat boiler
After the middle pressure steam of~4.4MPaG, the Process Gas that waste heat boiler 2 exports sequentially enters the second level gram labor in claus reaction system
This reactor 3, three-level claus reaction device 4 and selective catalytic oxidation reactor 5 generate sulphur and sulphur tail processed after reaction
Gas；
(2) 3.5~4.4MPaG middle pressure steam of by-product is made to enter the superheat section 8 of smoke convection room 7, with tail gas burning furnace 6
The 800 DEG C of flue gases generated exchange heat, and obtained middle pressure superheat steam temperature is 420 DEG C, the flue gas after the heat exchange of superheat section 8
Temperature is 650 DEG C, defeated outside hot steam by pressing through in after heat exchange；
(3) 132 from battery limit (BL) DEG C of medium-pressure boiler water supply are made to enter the boiler feedwater preheating section 9 of smoke convection room 7, with warp
It crosses 650 DEG C of flue gases after superheat section 8 exchanges heat to exchange heat, the boiler feed temperature after obtained preheating is 253 DEG C, by boiler
Flue-gas temperature after feed-water preheating section 9 exchanges heat is 460 DEG C, and the boiler feedwater after making preheating enters waste heat boiler 2；
(4) so that 122 DEG C of sulphur tail gas processed is entered the tail gas preheating section 10 of smoke convection room 7, preheated with by boiler feedwater
460 DEG C of flue gases after 9 heat exchange of section exchange heat, and the sulphur exhaust temperature processed after obtained preheating is 280 DEG C, by tail gas preheating section
Flue-gas temperature after 10 heat exchange is 360 DEG C, and so that the sulphur tail gas processed after preheating is entered tail gas burning furnace 6, while passing through fuel gas
Entrance is passed through fuel gas (i.e. natural gas) into tail gas burning furnace 6 and is passed through air into tail gas burning furnace 6 by air intake,
To be burned to sulphur tail gas processed；
(5) 20~40 DEG C of acid gas is made to enter the unstripped gas preheating section 11 of smoke convection room 7, and it is pre- by tail gas
360 DEG C of flue gases after hot arc 10 exchanges heat exchange heat, and the acid gas temperature after obtained preheating is 280 DEG C, by raw material
Flue-gas temperature after gas preheating section 11 exchanges heat is 266 DEG C, and the acid gas after making preheating enters burner for producing sulfur 1 and fired
It burns；
(6) normal temperature air from air blower 13 is made to enter the sulphur air preheat section 12 processed of smoke convection room 7, it is former with passing through
266 DEG C of flue gases after material gas preheating section 11 exchanges heat exchange heat, and the air themperature after obtained preheating is 280 DEG C, by sulphur processed
Flue-gas temperature after air preheat section 12 exchanges heat is 180 DEG C, and the air after making preheating enters burner for producing sulfur 1 for combustion acid
Unstripped gas；
(7) by 180 DEG C of flue gases after sulphur air preheat section 12 processed heat exchange (i.e. after heat is recycled in five sections of heat transfer zones
Flue gas) battery limit (BL) sent out by air-introduced machine 14 and chimney 15.
In energy-efficient sulfur recovery unit and method provided in this embodiment, it should be noted that, it brings into operation just
When the device of the present embodiment, acid gas and air into burner for producing sulfur be the acid gas that does not exchange heat and
Air runs a period of time to device, after generating sulphur tail gas and high-temperature flue gas processed, recycles flue gas to acid gas, sulphur processed
Air and sulphur tail gas processed etc. exchange heat, and acid gas, the sulphur air processed after heat exchange are sent into burner for producing sulfur.
Embodiment 2
Present embodiments provide a kind of energy-efficient sulfur recovery unit and method, as shown in Fig. 2, the structure of the device and
Process flow is substantially the same manner as Example 1, the difference is that: tail gas burning furnace 6 is connected the furnace to be formed with smoke convection room 7
Body be vertical incinerator withShape smoke convection room, which is connected, to be formedShape furnace body, the vertical incinerator are vertical
Rectangular incinerator.
Embodiment 3
Present embodiments provide a kind of energy-efficient sulfur recovery unit and method, as shown in figure 3, the structure of the device and
Process flow is substantially the same manner as Example 1, the difference is that: tail gas burning furnace 6 is connected the furnace to be formed with smoke convection room 7
Body is that horizontal incinerator and horizontal smoke convection room are coaxially connected the furnace body to be formed, which burns for horizontal cylindrical shape
Burn furnace.
Claims (8)
1. a kind of energy-efficient sulfur recovery unit comprising: thermal response system, claus reaction system and tail gas burn and
Flue gas heat recovery system；
Wherein, the thermal response system includes: burner for producing sulfur and waste heat boiler；
The tail gas burns and flue gas heat recovery system includes: that tail gas burning furnace is connected the furnace to be formed with smoke convection room
Body；The smoke convection room is provided with five sections of heat transfer zones, comprising: superheat section, boiler feedwater preheating section, tail gas preheating section, raw material
Gas preheating section and sulphur air preheat section processed；
Burner for producing sulfur in the thermal response system is connected to waste heat boiler, and the Process Gas outlet of the waste heat boiler passes through pipe
Line is connected to the claus reaction system；
The middle pressure saturated vapor outlet of the waste heat boiler is connected with the steam input pipe line of the superheat section of the smoke convection room
It connects, so that the flue gas that the middle pressure saturated vapor of waste heat boiler by-product is generated with the tail gas burning furnace exchanges heat, and will heat exchange
It is pressed through in afterwards defeated outside hot steam；
The boiler feedwater export pipeline phase of the admission port of the waste heat boiler and the boiler feedwater preheating section of the smoke convection room
Connection so that the medium-pressure boiler water supply from battery limit (BL) exchanges heat with the flue gas after superheat section exchanges heat, and makes after preheating
Medium-pressure boiler water supply enters waste heat boiler；
The tail gas input pipe of the tail gas preheating section of the sulphur offgas outlet processed and smoke convection room of the claus reaction system
One end of line is connected, and the other end of the tail gas intake pipeline is connected to the tail gas burning furnace, so that sulphur tail gas processed and warp
Flue gas after crossing the heat exchange of boiler feedwater preheating section exchanges heat, and so that the sulphur tail gas processed after preheating is entered tail gas burning furnace and burnt
It burns；
The acid gas of the acid gas entrance of the burner for producing sulfur and the unstripped gas preheating section of the smoke convection room
Intake pipeline connection so that acid gas exchanges heat with the flue gas after the heat exchange of tail gas preheating section, and makes after preheating
Acid gas enters burner for producing sulfur；
The air outlet line phase of the air intake of the burner for producing sulfur and the sulphur air preheat section processed of the smoke convection room
Connection so that air exchanges heat with the flue gas after the heat exchange of unstripped gas preheating section, and enters the sulphur air processed after preheating
Burner for producing sulfur；
The tail gas burning furnace is additionally provided with a fuel gas entrance and an air intake；
The energy-efficient sulfur recovery unit further includes that an at least air-introduced machine and an at least chimney, the chimney draw with described
Blower passes sequentially through the exhanst gas outlet that pipeline is connected to the smoke convection room, for will by sulphur air preheat section processed heat exchange after
Flue gas send out battery limit (BL).
2. energy-efficient sulfur recovery unit according to claim 1 further includes an at least air blower, the air blower
It is connected with the air inlet line of the sulphur air preheat section processed of the smoke convection room, for delivering the air to smoke convection room
Sulphur air preheat section processed with by unstripped gas preheating section heat exchange after flue gas exchange heat, and make preheating after air enter system
Sulphur burner.
3. energy-efficient sulfur recovery unit according to claim 1, wherein the claus reaction system includes: successively
Second level claus reaction device, three-level claus reaction device and the selective catalytic oxidation reactor connected by pipeline.
4. energy-efficient sulfur recovery unit according to claim 1, wherein the tail gas burning furnace and smoke convection room phase
The furnace body that connection is formed is that vertical incinerator is connected to be formed with horizontal smoke convection roomShape furnace body,
Or for vertical incinerator withShape smoke convection room, which is connected, to be formedShape furnace body,
Or coaxially it is connected the furnace body to be formed for horizontal incinerator and horizontal smoke convection room.
5. according to claim 1 or the 4 energy-efficient sulfur recovery units, wherein the tail gas burning furnace is vertical cylinder
Shape incinerator, vertical type square incinerator or horizontal cylindrical shape incinerator.
6. a kind of energy-efficient sulfur recovery method, uses energy-efficient sulphur of any of claims 1-5 to return
Receiving apparatus, method includes the following steps:
(1) make acid gas and sulphur air processed enter burner for producing sulfur to burn, combustion product enters waste heat boiler by-product
Middle pressure saturated vapor, then the Process Gas of waste heat boiler outlet enters claus reaction system, and sulphur and sulphur processed are generated after reaction
Tail gas；
(2) so that the middle pressure saturated vapor of by-product is entered the superheat section of smoke convection room, carried out with the flue gas that tail gas burning furnace generates
Heat exchange, and it is defeated outside hot steam by pressing through in after heat exchange；
(3) so that the medium-pressure boiler water supply from battery limit (BL) is entered the boiler feedwater preheating section of smoke convection room, changed with by superheat section
Flue gas after heat exchanges heat, and the boiler feedwater after preheating is made to enter waste heat boiler；
(4) sulphur tail gas processed is made to enter the tail gas preheating section of smoke convection room, with the flue gas after the heat exchange of boiler feedwater preheating section
It exchanges heat, and so that the sulphur tail gas processed after preheating is entered tail gas burning furnace, while being passed through fuel gas and sky into tail gas burning furnace
Gas, to be burned to sulphur tail gas processed；
(5) acid gas is made to enter the unstripped gas preheating section of smoke convection room, with the flue gas after the heat exchange of tail gas preheating section
It exchanges heat, and so that the acid gas after preheating is entered burner for producing sulfur and burn；
(6) the sulphur air preheat section processed for admitting air into smoke convection room, with by unstripped gas preheating section heat exchange after flue gas into
Row heat exchange, and the air after preheating is made to enter burner for producing sulfur for combustion acid unstripped gas；
(7) flue gas after sulphur air preheat section processed heat exchange is sent out into battery limit (BL).
7. energy-efficient sulfur recovery method according to claim 6, wherein the pressure of the middle pressure steam of waste heat boiler by-product
Power is 3.5~4.4MPaG.
8. energy-efficient sulfur recovery method according to claim 6, wherein tail gas burning furnace generate flue-gas temperature be
800~900 DEG C, after the heat exchange of the middle pressure steam of superheat section and waste heat boiler by-product, obtained middle pressure superheat steam temperature is 420
~450 DEG C, the flue-gas temperature after superheat section exchanges heat is 650~700 DEG C；
The temperature of medium-pressure boiler water supply from battery limit (BL) is 104 DEG C~132 DEG C, is changed in boiler feedwater preheating section with by superheat section
After 650~700 DEG C of flue gases after heat are exchanged heat, the boiler feed temperature after obtained preheating is 240~260 DEG C, by pot
Flue-gas temperature after the heat exchange of furnace feed-water preheating section is 460~500 DEG C；
The temperature of sulphur tail gas processed be 122~130 DEG C, tail gas preheating section with by boiler feedwater preheating section heat exchange after 460~
After 500 DEG C of flue gases are exchanged heat, the sulphur exhaust temperature processed after obtained preheating is 250~300 DEG C, is exchanged heat by tail gas preheating section
Flue-gas temperature afterwards is 350~400 DEG C；
Temperature into the acid gas of unstripped gas preheating section is 20~40 DEG C, is preheated in unstripped gas preheating section and by tail gas
After 350~400 DEG C of flue gases after Duan Huanre are exchanged heat, the acid gas temperature after obtained preheating is 250~300 DEG C,
Flue-gas temperature after the heat exchange of unstripped gas preheating section is 260~320 DEG C；
Temperature into the air of sulphur air preheat section processed is room temperature, is changed in sulphur air preheat section processed with by unstripped gas preheating section
After 260~320 DEG C of flue gases after heat are exchanged heat, the air themperature after obtained preheating is 250~300 DEG C, empty by sulphur processed
Flue-gas temperature after the heat exchange of gas preheating section is 180~240 DEG C.
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| CN107830538B (en) * | 2017-12-07 | 2023-06-30 | 南京宜热纵联环保科技溧阳有限公司 | Optimized indirect catalytic incineration flue gas multistage heat exchange system and process |
| CN108786370A (en) * | 2018-06-27 | 2018-11-13 | 山东大学 | It burns, the Sulphur ressource recovery method and device of parsing, carbon heat reducing coordination |
| CN110056890A (en) * | 2019-02-27 | 2019-07-26 | 洛阳瑞昌环境工程有限公司 | A kind of high-sulfur exhaust treatment system and technique |
| CN109911863A (en) * | 2019-04-23 | 2019-06-21 | 中国海洋石油集团有限公司 | A kind of Sulfur Recovery Equipment |
| CN115959633A (en) * | 2021-10-09 | 2023-04-14 | 中石化南京化工研究院有限公司 | Startup temperature rising system and startup temperature rising method of sulfuric acid preparation device |
| CN114735657B (en) * | 2022-04-22 | 2024-06-07 | 瑞切尔石化工程(上海)有限公司 | Condenser for sulfur production device, sulfur production device based on Claus method and sulfur production process |
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