CN114212759A - Production process of high-purity liquid sulfur trioxide - Google Patents
Production process of high-purity liquid sulfur trioxide Download PDFInfo
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- CN114212759A CN114212759A CN202111419958.0A CN202111419958A CN114212759A CN 114212759 A CN114212759 A CN 114212759A CN 202111419958 A CN202111419958 A CN 202111419958A CN 114212759 A CN114212759 A CN 114212759A
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- sulfur trioxide
- fuming acid
- acid
- fuming
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- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 title claims abstract description 124
- 239000007788 liquid Substances 0.000 title claims abstract description 34
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 25
- 239000002253 acid Substances 0.000 claims abstract description 61
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 43
- 238000010521 absorption reaction Methods 0.000 claims abstract description 32
- 238000007872 degassing Methods 0.000 claims abstract description 20
- 239000007789 gas Substances 0.000 claims abstract description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000003546 flue gas Substances 0.000 claims abstract description 16
- 238000000034 method Methods 0.000 claims abstract description 9
- 230000008569 process Effects 0.000 claims abstract description 9
- 239000012071 phase Substances 0.000 claims abstract description 8
- 238000003860 storage Methods 0.000 claims abstract description 8
- 239000007791 liquid phase Substances 0.000 claims abstract description 4
- 238000004064 recycling Methods 0.000 claims abstract description 4
- 238000005507 spraying Methods 0.000 claims abstract description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 230000009102 absorption Effects 0.000 abstract description 22
- 238000001704 evaporation Methods 0.000 abstract description 6
- 230000008020 evaporation Effects 0.000 abstract description 6
- 238000009833 condensation Methods 0.000 abstract description 3
- 230000005494 condensation Effects 0.000 abstract description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 5
- 235000003599 food sweetener Nutrition 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 238000006277 sulfonation reaction Methods 0.000 description 4
- 239000003765 sweetening agent Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- WBZFUFAFFUEMEI-UHFFFAOYSA-M Acesulfame k Chemical compound [K+].CC1=CC(=O)[N-]S(=O)(=O)O1 WBZFUFAFFUEMEI-UHFFFAOYSA-M 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 229960004998 acesulfame potassium Drugs 0.000 description 3
- 235000010358 acesulfame potassium Nutrition 0.000 description 3
- 239000000619 acesulfame-K Substances 0.000 description 3
- 229960005164 acesulfame Drugs 0.000 description 2
- YGCFIWIQZPHFLU-UHFFFAOYSA-N acesulfame Chemical compound CC1=CC(=O)NS(=O)(=O)O1 YGCFIWIQZPHFLU-UHFFFAOYSA-N 0.000 description 2
- 235000013373 food additive Nutrition 0.000 description 2
- 239000002778 food additive Substances 0.000 description 2
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 description 2
- XNGIFLGASWRNHJ-UHFFFAOYSA-N phthalic acid Chemical compound OC(=O)C1=CC=CC=C1C(O)=O XNGIFLGASWRNHJ-UHFFFAOYSA-N 0.000 description 2
- 235000019204 saccharin Nutrition 0.000 description 2
- CVHZOJJKTDOEJC-UHFFFAOYSA-N saccharin Chemical compound C1=CC=C2C(=O)NS(=O)(=O)C2=C1 CVHZOJJKTDOEJC-UHFFFAOYSA-N 0.000 description 2
- 229940081974 saccharin Drugs 0.000 description 2
- 239000000901 saccharin and its Na,K and Ca salt Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- HIFJUMGIHIZEPX-UHFFFAOYSA-N sulfuric acid;sulfur trioxide Chemical compound O=S(=O)=O.OS(O)(=O)=O HIFJUMGIHIZEPX-UHFFFAOYSA-N 0.000 description 2
- 239000000271 synthetic detergent Substances 0.000 description 2
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical class C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000004996 alkyl benzenes Chemical class 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 206010012601 diabetes mellitus Diseases 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005670 sulfation reaction Methods 0.000 description 1
- 235000019605 sweet taste sensations Nutrition 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
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Classifications
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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
- C01B17/90—Separation; Purification
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
A production process of high-purity liquid sulfur trioxide comprises the following steps: introducing flue gas generated by three sections of outlets in a sulfuric acid production process into a fuming acid absorption tower, spraying fuming acid to absorb sulfur trioxide, allowing the fuming acid after absorption to enter a fuming acid circulating tank, allowing one part of the fuming acid in the fuming acid circulating tank to continuously absorb sulfur trioxide through a fuming acid cooler, allowing the other part of the fuming acid to enter an evaporator for evaporation through a fuming acid preheater, returning the heated liquid phase to the fuming acid circulating tank for recycling, and condensing the gas phase at the evaporation position to obtain crude liquid sulfur trioxide; liquid sulfur trioxide enters the upper part of the degassing tower, dry air enters the degassing tower from the lower part of the degassing tower, and the liquid sulfur trioxide after degassing treatment enters a sulfur trioxide storage tank for storage. The process adopts absorption, evaporation, condensation and degassing processes to absorb, produce and purify the sulfur trioxide, thereby improving the purity of the sulfur trioxide.
Description
Technical Field
The invention relates to a production process of high-purity liquid sulfur trioxide.
Background
Liquid sulfur trioxide not only has the same performance as sulfuric acid and oleum, but also has better performances in the industries of synthetic detergents, dyes, petroleum processing, synthetic fibers, medicines, pesticides and the like than concentrated sulfuric acid and oleum, and the liquid sulfur trioxide not only has a company or a mechanism for specially researching the production and application technology of liquid sulfur trioxide, but also has a plurality of production departments for applying the liquid sulfur trioxide to industrial production by replacing the oleum with the liquid sulfur trioxide. For example, the sulfonation of alkylbenzenes in the production of synthetic detergents; sulfonation and sulfation reactions of higher alcohols and ethylene oxide adducts; sulfonation of lube oil fractions in petroleum refining; sulfonation of aromatic compounds such as benzene, toluene, xylene, nitrobenzene, phthalic acid, and the like, has been accomplished by using liquid sulfur trioxide in place of oleum.
In the reaction of fuming sulfuric acid, a large amount of waste acid can be generated, the treatment of the waste acid can cause certain influence on the environment, the sulfur trioxide replaces the fuming sulfuric acid to participate in the reaction, the waste acid is not generated, and the problem of waste acid treatment in production is fundamentally solved.
In recent years, because of the importance on the health of people, sugar-substituting products are popularized and applied. Acesulfame potassium, formula: c4H4KNO4S, chemical, is a food additive. Similar to saccharin, the saccharin is easy to dissolve in water, can increase the sweet taste of food, has no nutrition, good mouthfeel, does not have calorie, has the characteristics of no metabolism and no absorption in a human body (being an ideal sweetener for middle-aged and elderly people, obese patients and diabetic patients), has good heat and acid stability and the like, and is a fourth-generation synthetic sweetener in the world at present. The sweetener can generate strong synergistic effect when being mixed with other sweeteners, and can increase the sweetness by 30-50% under the common concentration. The liquid sulfur trioxide is needed in the production of the acesulfame potassium, the food additive has high requirements on the quality of the sulfur trioxide, and the common liquid sulfur trioxide contains reducing substances such as sulfur dioxide and the like and impurities, which do not meet the production requirements of the acesulfame potassium.
Since sulfur trioxide is required for the production of both acesulfame and sulfuric acid, the production of sulfuric acid is also performed in general production plants for acesulfame in order to effectively utilize resources.
Disclosure of Invention
The invention aims to solve the technical problem of providing a production process of high-purity liquid sulfur trioxide, which adopts absorption, evaporation, condensation and degassing processes to absorb, produce and purify sulfur trioxide, thereby improving the purity of the sulfur trioxide.
In order to solve the technical problem, the invention provides a production process of high-purity liquid sulfur trioxide, which comprises the following steps:
(1) introducing flue gas generated by three sections of outlets in a sulfuric acid production process into a fuming acid absorption tower, spraying and absorbing sulfur trioxide in the flue gas by using fuming acid, allowing the absorbed fuming acid to enter a fuming acid circulating tank, and allowing unabsorbed gas phase to enter a first absorption tower;
(2) cooling a part of fuming acid in the fuming acid circulating tank to 35-44 ℃ by using a fuming acid cooler, continuously absorbing sulfur trioxide by using the fuming acid cooler as a spray liquid of a fuming acid absorption tower, and heating the other part of the fuming acid in the fuming acid circulating tank to 90 ℃ by using a fuming acid preheater;
(3) the preheated fuming acid enters an evaporator and is continuously heated to 120-140 ℃ to be evaporated, the heated liquid phase returns to a fuming acid circulating tank for recycling, and evaporated gaseous sulfur trioxide enters a cooler to be condensed to obtain crude liquid sulfur trioxide;
(4) liquid sulfur trioxide enters the upper part of the degassing tower, the drying air at the temperature of 43 ℃ enters the lower part of the degassing tower, the liquid sulfur trioxide after degassing treatment enters the sulfur trioxide storage tank for storage, and the gas phase discharged by the degassing tower is absorbed by the second absorption tower.
Preferably, the heat source of the evaporator is high-temperature flue gas at the outlet of the low-temperature superheater in the sulfuric acid production line, the tail gas of the high-temperature flue gas passing through the evaporator is absorbed by an absorption tower of a sulfuric acid section, and the tail gas is absorbed by a desulfurization tower and then is discharged.
Preferably, the first absorption tower and the second absorption tower are both absorption towers of a sulfuric acid section.
For the sake of simplicity of explanation, the process for producing high-purity liquid sulfur trioxide according to the present invention will be referred to as the present process hereinafter.
The process has the advantages that: the process adopts absorption, evaporation, condensation and degassing processes to absorb, produce and purify the sulfur trioxide, and solves the problem of high content of sulfur trioxide reduction products and impurities in the prior art.
The flue gas generated by the three-section outlet in the sulfuric acid production process is mainly sulfur trioxide, sulfur dioxide which is not converted into sulfur trioxide and partial impurities, and the first absorption tower absorbs partial sulfur dioxide which is not converted into sulfur trioxide and can enter a sulfuric acid working section to continuously participate in the reaction;
the gas phase discharged by the sulfur trioxide degassing tower is gaseous sulfur trioxide and partial impurity gas, and can also enter a sulfuric acid working section to participate in reaction;
the flue gas temperature at the outlet of the low-temperature superheater in the sulfuric acid production line can reach 350 ℃, the flue gas enters the evaporator as a heat source, the fuming acid is heated to generate gaseous sulfur trioxide, the heating mode can save energy, and the tail gas contains sulfur dioxide and sulfur trioxide, so that the tail gas can enter a sulfuric acid working section to continuously participate in reaction, and the resource utilization rate is maximized.
Drawings
FIG. 1 is a schematic flow diagram of the process.
Detailed Description
Referring to fig. 1, a process for producing high-purity liquid sulfur trioxide comprises the following steps:
(1) introducing flue gas generated by three-section outlets in a sulfuric acid production process into a fuming acid absorption tower, spraying and absorbing sulfur trioxide in the flue gas by using fuming acid, allowing the absorbed fuming acid to enter a fuming acid circulating groove (the fuming acid with the concentration of absorbing acid which is discharged into the fuming acid circulating groove by the fuming acid absorption tower being 104.5%), and allowing unabsorbed gas phase to enter a first absorption tower;
(2) cooling a part of fuming acid in the fuming acid circulating tank to 35-44 ℃ by using a fuming acid cooler, continuously absorbing sulfur trioxide by using the fuming acid cooler as a spray liquid of a fuming acid absorption tower, and heating the other part of the fuming acid in the fuming acid circulating tank to 90 ℃ by using a fuming acid preheater;
(3) the preheated fuming acid enters an evaporator and is continuously heated to 120-140 ℃ to be evaporated, the heated liquid phase returns to a fuming acid circulating tank for recycling, and gaseous sulfur trioxide at the evaporation position enters a cooler to be condensed to obtain crude liquid sulfur trioxide;
(4) liquid sulfur trioxide enters the upper part of the degassing tower, the drying air at the temperature of 43 ℃ enters the lower part of the degassing tower, the liquid sulfur trioxide after degassing treatment enters the sulfur trioxide storage tank for storage, and the gas phase discharged by the degassing tower is absorbed by the second absorption tower.
The heat source of the evaporator is high-temperature flue gas at the outlet of the low-temperature superheater in the sulfuric acid production line, the tail gas of the high-temperature flue gas is absorbed by an absorption tower of a sulfuric acid working section after passing through the evaporator, and the tail gas is absorbed by a desulfurization tower and then is discharged.
The first absorption tower and the second absorption tower are both absorption towers of a sulfuric acid working section.
Claims (3)
1. A production process of high-purity liquid sulfur trioxide is characterized by comprising the following steps:
(1) introducing flue gas generated by three sections of outlets in a sulfuric acid production process into a fuming acid absorption tower, spraying and absorbing sulfur trioxide in the flue gas by using fuming acid, allowing the absorbed fuming acid to enter a fuming acid circulating tank, and allowing unabsorbed gas phase to enter a first absorption tower;
(2) cooling a part of fuming acid in the fuming acid circulating tank to 35-44 ℃ by using a fuming acid cooler, continuously absorbing sulfur trioxide by using the fuming acid cooler as a spray liquid of a fuming acid absorption tower, and heating the other part of the fuming acid in the fuming acid circulating tank to 90 ℃ by using a fuming acid preheater;
(3) the preheated fuming acid enters an evaporator and is continuously heated to 120-140 ℃ to be evaporated, the heated liquid phase returns to a fuming acid circulating tank for recycling, and evaporated gaseous sulfur trioxide enters a cooler to be condensed to obtain crude liquid sulfur trioxide;
(4) liquid sulfur trioxide enters the upper part of the degassing tower, the drying air at the temperature of 43 ℃ enters the lower part of the degassing tower, the liquid sulfur trioxide after degassing treatment enters the sulfur trioxide storage tank for storage, and the gas phase discharged by the degassing tower is absorbed by the second absorption tower.
2. The process for producing high-purity liquid sulfur trioxide according to claim 1, characterized in that: the heat source of the evaporator is high-temperature flue gas at the outlet of the low-temperature superheater in the sulfuric acid production line, the tail gas of the high-temperature flue gas is absorbed by an absorption tower of a sulfuric acid working section after passing through the evaporator, and the tail gas is absorbed by a desulfurization tower and then is discharged.
3. The process for producing high-purity liquid sulfur trioxide according to claim 1, characterized in that: the first absorption tower and the second absorption tower are both absorption towers of a sulfuric acid working section.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111419958.0A CN114212759A (en) | 2021-11-26 | 2021-11-26 | Production process of high-purity liquid sulfur trioxide |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111419958.0A CN114212759A (en) | 2021-11-26 | 2021-11-26 | Production process of high-purity liquid sulfur trioxide |
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| CN114212759A true CN114212759A (en) | 2022-03-22 |
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| CN202111419958.0A Pending CN114212759A (en) | 2021-11-26 | 2021-11-26 | Production process of high-purity liquid sulfur trioxide |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115057415A (en) * | 2022-06-13 | 2022-09-16 | 湖北龙祥磷化有限公司 | Production process of high-purity electronic acid |
| CN115448259A (en) * | 2022-07-22 | 2022-12-09 | 江化微(镇江)电子材料有限公司 | Production method of electronic-grade sulfuric acid |
| 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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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101683973A (en) * | 2008-09-12 | 2010-03-31 | 赫多特普索化工设备公司 | Process for the production of sulphuric acid |
| CN101759156A (en) * | 2010-01-06 | 2010-06-30 | 山东聊城鲁西化工第六化肥有限公司 | Two-stage absorption process of fuming sulfuric acid system and equipment thereof |
| CN103407972A (en) * | 2013-08-06 | 2013-11-27 | 上海正帆科技有限公司 | Production method of electronic-grade sulphuric acid |
| CN104211020A (en) * | 2014-08-21 | 2014-12-17 | 山东聊城鲁西化工第六化肥有限公司 | Regulating process for diversification of products produced by sulfuric acid plant |
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2021
- 2021-11-26 CN CN202111419958.0A patent/CN114212759A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101683973A (en) * | 2008-09-12 | 2010-03-31 | 赫多特普索化工设备公司 | Process for the production of sulphuric acid |
| CN101759156A (en) * | 2010-01-06 | 2010-06-30 | 山东聊城鲁西化工第六化肥有限公司 | Two-stage absorption process of fuming sulfuric acid system and equipment thereof |
| CN103407972A (en) * | 2013-08-06 | 2013-11-27 | 上海正帆科技有限公司 | Production method of electronic-grade sulphuric acid |
| CN104211020A (en) * | 2014-08-21 | 2014-12-17 | 山东聊城鲁西化工第六化肥有限公司 | Regulating process for diversification of products produced by sulfuric acid plant |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115057415A (en) * | 2022-06-13 | 2022-09-16 | 湖北龙祥磷化有限公司 | Production process of high-purity electronic acid |
| CN115448259A (en) * | 2022-07-22 | 2022-12-09 | 江化微(镇江)电子材料有限公司 | Production method of electronic-grade sulfuric acid |
| 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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Application publication date: 20220322 |