CN109319743A - A kind of letter method energy efficiency extracting sulfuric acid technique - Google Patents
A kind of letter method energy efficiency extracting sulfuric acid technique Download PDFInfo
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- CN109319743A CN109319743A CN201710668528.XA CN201710668528A CN109319743A CN 109319743 A CN109319743 A CN 109319743A CN 201710668528 A CN201710668528 A CN 201710668528A CN 109319743 A CN109319743 A CN 109319743A
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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
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
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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
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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 relates to a kind of simple method energy efficiency extracting sulfuric acid techniques, after air is filtered by air filter, it is removed water in into drying tower, such as sulfur furnace and Molten sulphur after atomization is sent to burn in furnace by main air blower pressurization, sulphur oxidation generates SO2 flue gas, kiln gas enters one section of converter and is converted out, flue gas is oxidized to SO3 under the action of catalyst, one section of flue gas is after one section of waste heat boiler cools down out, into two sections of catalysis oxidations of converter, two sections come out flue gas after high temperature superheater cools down, into three sections of catalysis oxidations of converter, three sections of exiting flue gas successively pass through low temperature superheater and economizer is cooled to 200 DEG C or so and enters the absorption tower RHS, RHS tail gas from absorption tower enters ionic liquid desulfuration absorbing tower, SO2 gas absorption is deviate from, tail gas up to standard is discharged from tower top chimney；The SO2 absorbed is sent to drying tower import after parsing in ionic liquid desulfurization Analytic Tower and goes out, and uses as relieving haperacidity unstripped gas, economizes on resources while also protecting environment.
Description
Technical field
The present invention relates to sulfuric acid manufacturing process area, specifically a kind of letter method energy efficiency extracting sulfuric acid technique.
Background technique
Country's acid production with sulphur technique is substantially double-absorption technique at present, and primary conversion is divided into three sections, after three sections of conversions
Then it absorbs for the first time, secondary conversion is divided into two sections, two sections of conversions followed by second of absorption.For main technique as schemed, air is logical
After crossing air filter filtering, into drying tower in dry water removal, made a gift to someone liquid after sulfur furnace and atomization by air-blaster pressurization
Body sulphur burns in furnace, and sulphur oxidation generates SO2 flue gas.Flue-gas temperature is up to 1050 DEG C or so in sulfur furnace, out kiln gas
420 DEG C are cooled to from 1050 DEG C by shell-and-tube waste heat, is converted into one section of converter, SO2 gas is converted into SO3 gas
Body, conversion one section outlet furnace gas are cooled to 420 DEG C from 610 DEG C by high temperature superheater.High temperature superheater comes out flue gas entrance and turns
Change two sections of device to continue to convert, converter second stage exit flue gas is cooled to 420 DEG C or so through overheat heat exchanger heat exchange cooling, flue gas
Into three sections of converter, three sections of converter come out flue gas and cool by hot and cold heat exchanger and economizer II to 175 DEG C or so
Into the first absorption tower, SO3 gas being absorbed with 98% concentrated sulfuric acid in the first absorption tower, the concentrated sulfuric acid being made, this process is primary turns
Change an absorption process.The first adsorption tower smoke continues second of conversion and second of absorption out, out the first absorption tower cigarette
Gas successively heats to 420 DEG C via hot and cold heat exchanger and Re Re heat exchange and enters four sections of converter, four sections of outlet cigarettes of converter
Gas through medium temperature overheater be cooled to 420 DEG C or so enter five sections of converter, after catalysis oxidation 430 DEG C or so flue gases go out converter into
Enter low temperature superheater and economizer I successively cools to 160 DEG C, is sent into second absorption tower and carries out second of absorption, whole process claims
Be double conversion double absorption.The flue gas that second absorption tower comes out, which contains, fails to absorb ability row up to standard after complete SO2 gas needs are handled
It puts, flue gas is discharged into tail gas funnel emptying after initially entering desulfuration absorbing tower desulfurization.Traditional sulfur method mainly have alkali desulphurization,
Peroxide passivation desulfurization etc. has secondary pollution or generates diluted acid although flue gas after desulfurization can reach International Environmental Protection requirement after desulfurization
The problems such as
Summary of the invention
It is an object of the present invention to provide a kind of novel simple method energy efficiency extracting sulfuric acid techniques, to solve to deposit in the prior art
Defect.
The technical scheme to solve the above technical problems is that
A kind of novel simple method energy efficiency extracting sulfuric acid technique, firstly, after air is filtered by air filter (20),
Dry water removal in into drying tower (19) is pressurized by main air blower (1) and is sent into sulfur furnace (2) with Molten sulphur after atomization in sulfur furnace
(2) burning in, sulphur oxidation generate SO2 flue gas, and sulfur furnace (2) interior flue-gas temperature is up to 1050 DEG C or so, and kiln gas passes through out
Waste heat boiler (3) is cooled to 420 DEG C from 1050 DEG C, is converted into (4) one sections of converter, flue gas oxygen under the action of catalyst
It is melted into SO3, one section of flue gas is after one section of waste heat boiler (5) cools down out, and into (4) two sections of catalysis oxidations of converter, two sections are come out
Flue gas is after high temperature superheater (6) cool down, and into (4) three sections of catalysis oxidations of converter, three sections of exiting flue gas successively pass through low temperature
Superheater (7) and economizer (8) are cooled to 200 DEG C or so and enter the absorption tower RHS (9) (the of this suitable double-absorption of tower function
One absorption tower), SO3 gas being absorbed with 99% concentrated sulfuric acid in the absorption tower RHS (9), the concentrated sulfuric acid being made, this process is one turn of one suction
Technique, the absorption tower RHS (9) tail gas enter ionic liquid desulfuration absorbing tower (17), SO2 gas absorption are deviate from, and tail gas up to standard is from tower
Push up chimney discharge.The SO2 absorbed is parsed in the ionic liquid desulfurization Analytic Tower (16), parse SO2 gas be sent to it is dry
Dry tower (19) import, uses as relieving haperacidity unstripped gas；
Further, the low-temperature flue gas that the absorption tower RHS (9) generates is through RHS steam generator (11) and extraneous addition
Deaerated water mixing in the RHS mixer (10), be delivered in the absorption tower RHS (9) after generating low-pressure saturated steam；With further
It is recycled to by low temperature position waste heat in sulphuric acid process, every one ton of 100% sulfuric acid by-product, 0.473 ton of low pressure saturation that produces is steamed
Vapour: heat recovery system (abbreviation RHS system), than the quantity of steam of traditional acid-making process fecund about 38%；
Further, the low-temperature flue gas that the absorption tower RHS (9) generates also pass sequentially through RHS deoxygenation water heater (12),
Enter in drying tower pump slot (14) after RHS desalination water heater (13) processing, with the softened water being added in drying tower pump slot (14)
Reaction generates the concentrated sulfuric acid, then by drying tower acid cooler (15), the concentrated sulfuric acid of generation after finished product acid cooler (18), output at
Product acid；Remaining flue gas continues to participate in acid manufacturing processes by main air blower (1) after drying tower (19).
The beneficial effects of the present invention are: equipment is reduced in entire technical solution production process, so that operating cost drops
Low, equipment investment total value reduces 10%, and corresponding occupied area is also reduced, and entire process flow is shortened, while being returned to waste heat
It receives, the SO2 Gas recovery in tail gas saves cost.
Detailed description of the invention
Fig. 1 is extracting sulfuric acid apparatus structure schematic diagram of the present invention；
In attached drawing, parts list represented by the reference numerals are as follows:
1, main air blower；2, sulfur furnace；3, waste heat boiler；4, converter；5, one section of waste heat boiler；6, high-pressure superheater；7,
Low temperature superheater；8, economizer；9, the absorption tower RHS；10, RHS mixer；11, RHS steam generator；12, RHS deaerated water adds
Hot device；13, RHS desalination water heater；14, drying tower pumps slot；15, drying tower acid cooler；16, ionic liquid desulfurization Analytic Tower；17,
Ionic liquid desulfuration absorbing tower；18, finished product acid cooler；19, drying tower；20, air filter.
Specific embodiment
1 pair of present invention process process is introduced with reference to the accompanying drawing, and simple method process for preparing sulfuric acid is mainly with respect to traditional
For double-absorption acid-making process, simple method relieving haperacidity only once converts an absorption process, without secondary conversion and secondary suction
Receipts process, entire acid-making process process are compact simple and direct.Main flow such as Fig. 1, a kind of novel simple method energy efficiency extracting sulfuric acid
Technique, firstly, after air is filtered by air filter (20), into drying tower (19) in dry water removal, increased by main air blower (1)
Force feed enters Molten sulphur burning in sulfur furnace (2) after sulfur furnace (2) and atomization, and sulphur oxidation generates SO2 flue gas, sulfur furnace
(2) interior flue-gas temperature is up to 1050 DEG C or so, and kiln gas from 1050 DEG C is cooled to 420 DEG C by waste heat boiler (3) out, into turning
Change (4) one sections of device to be converted, flue gas is oxidized to SO3 under the action of catalyst, and one section of flue gas is dropped through one section of waste heat boiler (5) out
Wen Hou, into (4) two sections of catalysis oxidations of converter, two sections come out flue gas after high temperature superheater (6) cooling, into converter
(4) three sections of catalysis oxidations, three sections of exiting flue gas successively pass through low temperature superheater (7) and economizer (8) be cooled to 200 DEG C or so into
Enter the absorption tower RHS (9) (the first absorption tower of this suitable double-absorption of tower function), with 99% concentrated sulfuric acid in the absorption tower RHS (9)
It absorbs SO3 gas and the concentrated sulfuric acid is made, this process is one turn of one suction technique, and the absorption tower RHS (9) tail gas enters ionic liquid desulfurization absorption
Tower (17), SO2 gas absorption is deviate from, and tail gas up to standard is discharged from tower top chimney.The SO2 absorbed is parsed in ionic liquid desulfurization
It is parsed in tower (16), parses SO2 gas and be sent to drying tower (19) import, used as relieving haperacidity unstripped gas；
Further, the low-temperature flue gas that the absorption tower RHS (9) generates is through RHS steam generator (11) and extraneous addition
Deaerated water mixing in the RHS mixer (10), be delivered in the absorption tower RHS (9) after generating low-pressure saturated steam；With further
It is recycled to by low temperature position waste heat in sulphuric acid process, every one ton of 100% sulfuric acid by-product, 0.473 ton of low pressure saturation that produces is steamed
Vapour: heat recovery system (abbreviation RHS system), than the quantity of steam of traditional acid-making process fecund about 38%；
Further, the low-temperature flue gas that the absorption tower RHS (9) generates also pass sequentially through RHS deoxygenation water heater (12),
Enter in drying tower pump slot (14) after RHS desalination water heater (13) processing, with the softened water being added in drying tower pump slot (14)
Reaction generates the concentrated sulfuric acid, then by drying tower acid cooler (15), the concentrated sulfuric acid of generation after finished product acid cooler (18), output at
Product acid；Remaining flue gas continues to participate in acid manufacturing processes by main air blower (1) after drying tower (19).
Technical solution of the present invention has the advantages that
1, production process equipment is reduced:
A converter is simplified only have three sections of conversions (while Catalyst packing reduction) by five sections of conversions.
Medium temperature overheater, hot heat exchanger and hot and cold heat exchanger after five sections of b conversions all do not have.
C double absorption system does not all have, including second absorption tower, sour circulating slot, acid circulating pump, acid cooler etc..
2, operating cost reduces:
A does not have secondary conversion and double absorption acid-making process process to shorten, drag reduction 10kPa of air blower or so, drum
Blower power consumption is reduced.
B is without second absorption tower acid circulating pump, this acid circulating pump is also just without operating cost.
3, equipment investment total value reduces 10% or so.
4, after equipment is reduced, whole device occupied area is accordingly reduced.
5, simple legal system sulfur process process is short, and plant personnel required is accordingly reduced, and saves management cost and personnel cost.
6, the first absorption tower is replaced using RHS heat recovery tower in simple method acid-making process, by low temperature in sulphuric acid process
Position waste heat is recycled (high temperature and middle potential temperature waste heat are generally recycled), passes through high-temperature high concentration sulfuric acid cyclic absorption
SO3 gas, lower tower acid generate steam, one ton of 100% sulfuric acid by-product 0.473 of every production by RHS steam generator heating deaerated water
Ton low-pressure saturated steam: heat recovery system (abbreviation RHS system), than the quantity of steam of traditional acid-making process fecund about 38%.
7, traditional desulphurization system, ionic liquid desulfurization are replaced using ionic liquid desulfurization in simple legal system acid process tail gas processing part
Using enfleurage pyrolytic process, SO2 gas abjection in tail gas is converted to raw material to be used, this method is to turn waste into wealth, will not
Reproducible Sulphur ressource recycles.Ionic liquid desulphurization system intermediate ion liquid, that is, SO2 gas circulating absorption solution, this ionic liquid are the
Three generation products reliable and stable can be run
The foregoing is merely presently preferred embodiments of the present invention, is not intended to limit the invention, it is all in spirit of the invention and
Within principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (3)
1. a kind of letter method energy efficiency extracting sulfuric acid technique, it is characterised in that: firstly, air is filtered by air filter (20)
Afterwards, into water removal dry in drying tower (19), it is pressurized Molten sulphur after being sent into sulfur furnace (2) and being atomized by main air blower (1) and is burning
Burning in sulphur furnace (2), sulphur oxidation generate SO2 flue gas, and sulfur furnace (2) interior flue-gas temperature is up to 1050 DEG C or so, out kiln gas
420 DEG C are cooled to from 1050 DEG C by waste heat boiler (3), is converted into (4) one sections of converter, flue gas is in catalyst action
Under be oxidized to SO3, one section of flue gas is after one section of waste heat boiler (5) cools down out, into (4) two sections of catalysis oxidations of converter, two sections
Flue gas is after high temperature superheater (6) cooling out, and into (4) three sections of catalysis oxidations of converter, three sections of exiting flue gas successively pass through
Low temperature superheater (7) and economizer (8) are cooled to 200 DEG C or so and enter the absorption tower RHS (9), use in the absorption tower RHS (9)
99% concentrated sulfuric acid absorbs SO3 gas and the concentrated sulfuric acid is made, this process is one turn of one suction technique, and the absorption tower RHS (9) tail gas enters ion
Liquid desulfuration absorbing tower (17), SO2 gas absorption is deviate from, and tail gas up to standard is discharged from tower top chimney, and the SO2 absorbed is in ion
It is parsed in liquid desulfurization Analytic Tower (16), parses SO2 gas and be sent to drying tower (19) import, make as relieving haperacidity unstripped gas
With.
2. letter method energy efficiency extracting sulfuric acid technique according to claim 1, it is characterised in that: the absorption tower RHS (9)
The low-temperature flue gas of generation mixes in RHS mixer (10) through RHS steam generator (11) with the deaerated water that the external world is added, and generates
It is delivered to after low-pressure saturated steam in the absorption tower RHS (9), further to be returned to by low temperature position waste heat in sulphuric acid process
It receives.
3. letter method energy efficiency extracting sulfuric acid technique according to claim 2, it is characterised in that: the absorption tower RHS (9)
The low-temperature flue gas of generation enters drying after also passing sequentially through RHS deoxygenation water heater (12), RHS desalination water heater (13) processing
Tower pumps in slot (14), reacts with the softened water being added in drying tower pump slot (14) and generates the concentrated sulfuric acid, then passes through drying tower acid cooler
(15), the concentrated sulfuric acid of generation is after finished product acid cooler (18), output finished acid；Remaining flue gas leads to after drying tower (19)
It crosses main air blower (1) and continues to participate in acid manufacturing processes.
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| CN201710668528.XA CN109319743A (en) | 2017-08-01 | 2017-08-01 | A kind of letter method energy efficiency extracting sulfuric acid technique |
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| CN201710668528.XA CN109319743A (en) | 2017-08-01 | 2017-08-01 | A kind of letter method energy efficiency extracting sulfuric acid technique |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109867267A (en) * | 2019-04-25 | 2019-06-11 | 吉林隆源骐化工有限责任公司 | A kind of conversion temperature elevation system in contact acid process units |
| CN110316704A (en) * | 2019-04-11 | 2019-10-11 | 湖北锦泽环保科技有限公司 | A kind of acid production with sulphur industrial tail gas technique of zero discharge |
| CN110885065A (en) * | 2019-12-18 | 2020-03-17 | 河南豫光锌业有限公司 | Method for roasting zinc sulfide concentrate and starting system of flue gas acid making system |
| CN111252743A (en) * | 2020-04-01 | 2020-06-09 | 中化重庆涪陵化工有限公司 | Sulfur acid making system for recovering low-level heat of secondary absorption process |
| CN111268653A (en) * | 2020-03-11 | 2020-06-12 | 上海乐谦工程科技有限公司 | Energy-saving conversion device and process for preparing sulfuric acid from sulfur-containing flue gas |
| CN116654876A (en) * | 2023-07-28 | 2023-08-29 | 潍坊春源化工有限公司 | Process and equipment for producing less sulfuric acid and more sulfur trioxide |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110316704A (en) * | 2019-04-11 | 2019-10-11 | 湖北锦泽环保科技有限公司 | A kind of acid production with sulphur industrial tail gas technique of zero discharge |
| CN109867267A (en) * | 2019-04-25 | 2019-06-11 | 吉林隆源骐化工有限责任公司 | A kind of conversion temperature elevation system in contact acid process units |
| CN110885065A (en) * | 2019-12-18 | 2020-03-17 | 河南豫光锌业有限公司 | Method for roasting zinc sulfide concentrate and starting system of flue gas acid making system |
| CN111268653A (en) * | 2020-03-11 | 2020-06-12 | 上海乐谦工程科技有限公司 | Energy-saving conversion device and process for preparing sulfuric acid from sulfur-containing flue gas |
| CN111252743A (en) * | 2020-04-01 | 2020-06-09 | 中化重庆涪陵化工有限公司 | Sulfur acid making system for recovering low-level heat of secondary absorption process |
| CN111252743B (en) * | 2020-04-01 | 2021-05-28 | 中化重庆涪陵化工有限公司 | Sulfur acid making system for recovering low-level heat of secondary absorption process |
| CN116654876A (en) * | 2023-07-28 | 2023-08-29 | 潍坊春源化工有限公司 | Process and equipment for producing less sulfuric acid and more sulfur trioxide |
| CN116654876B (en) * | 2023-07-28 | 2024-03-08 | 潍坊春源化工有限公司 | Process and equipment for producing less sulfuric acid and more sulfur trioxide |
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