CN210675125U - Shift catalyst intensification vulcanization system - Google Patents
Shift catalyst intensification vulcanization system Download PDFInfo
- Publication number
- CN210675125U CN210675125U CN201921306908.XU CN201921306908U CN210675125U CN 210675125 U CN210675125 U CN 210675125U CN 201921306908 U CN201921306908 U CN 201921306908U CN 210675125 U CN210675125 U CN 210675125U
- Authority
- CN
- China
- Prior art keywords
- gas
- vulcanization
- enters
- outlet
- combustion furnace
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- 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
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
The utility model relates to the field of shift catalyst warming and vulcanizing, in particular to a shift catalyst warming and vulcanizing system which organically combines shift vulcanization and Tuo ordinary process; organically combining the transformation vulcanization and the Tuopus process; one path of the outlet material of the combustion furnace enters a shift converter for vulcanization, nitrogen gas does not need to be supplemented and a new heat source does not need to be introduced in the vulcanization process, flue gas at the temperature of 850 ℃ and 0.1MPa of the combustion furnace is introduced, the use of a pressure raising device is reduced, the heat source does not need to be introduced in the process, the cost is reduced, the service life of equipment is prolonged, and the other path of the outlet material enters a Topyo acid making reactor through a waste heat recovery pipeline for sulfur dioxide conversion; the flue gas introduced from the outlet of the combustion furnace in the acid making process of the Topusol is used for replacing a 2.5MPa waste pot to heat gas in the temperature rising process, so that the vulcanization temperature is increased, the activity of a conversion catalyst is effectively activated, the cracking of a welded junction is avoided, the long-period stable operation of a system is ensured, and the problems of easy leakage of the 2.5MPa waste pot and poor vulcanization effect of the catalyst are thoroughly solved.
Description
Technical Field
The utility model relates to a transform catalyst intensification vulcanization technical field, more specifically relates to a transform catalyst intensification vulcanization system.
Background
The operation of transforming catalyst heating and sulfurizing includes four stages, heating, initial sulfurizing stage, main sulfurizing stage and cooling stage. The Roots machine will reduce the content of CS at high concentration at about 50 deg.C2N of (A)2The pressure is increased to about 45kPa, the waste heat is indirectly heated by a waste boiler with the pressure of 2.5MPa and then sent into a shift converter, and the shift catalyst is heated and vulcanized. Containing CS2N of (A)2The tube pass is adopted, and the superheated steam at about 430 ℃ is adopted in the shell pass. The hydrogen sulfide in the sulfuration process seriously corrodes the 2.5MPa waste boiler. The waste pot with 2.5MPa is used as a heating source, the maximum vulcanization temperature of the shift converter can only reach 320 ℃, and the requirement of a vulcanization strengthening period of 380-400 ℃ required by a vulcanization scheme can not be met, so that the catalyst has poor vulcanization effect and activity. The waste boiler has the function that high-temperature gas in the pipe heats desalted water between the pipes to generate steam, and the waste boiler with the pressure of 2.5MPa is about 100 ten thousand yuan, so that the waste boiler can be maintained for half a year. The vulcanization process is not affected by water, which is equivalent to dry burning, and the service life of the equipment is greatly reduced. The normal flow is that the pressure in the pipe is higher than the pressure outside the pipe, and the pressure outside the pipe is far higher than the pressure in the pipe during vulcanization, so that the welded junction is easy to crack. During vulcanization, a roots machine is required to be independently started to increase pressure, normal production is not required, equipment investment and maintenance cost are increased, and electric energy is consumed during vulcanization.
SUMMERY OF THE UTILITY MODEL
In order to overcome exist not enough among the prior art, the utility model provides a transform catalyst intensification vulcanization system improves transform catalyst intensification vulcanization temperature, guarantees that the catalyst uses the activity, realizes system waste gas used heat utilization as resources.
In order to solve the technical problem, the utility model discloses the technical scheme who adopts is:
a shift catalyst temperature-rising vulcanizing system comprises a shift converter, a water cooler, a gas-liquid separator, a combustion furnace, a Topusol acid-making reactor and a heat energy recovery system; one path of the outlet of the combustion furnace enters a shift converter for shift catalyst vulcanization reaction, and the other path of the outlet of the combustion furnace enters a heat energy recovery system through a waste heat recovery pipeline for recovering heat; one path of the outlet of the shift converter enters a waste heat recovery pipeline, and the other path of the outlet of the shift converter enters a water cooler; the outlet of the water cooler enters a gas-liquid separator; the gas phase of the gas-liquid separator enters a waste heat recovery pipeline, and the liquid phase discharges sewage; the heat recovery system uses the heat in the waste heat recovery pipeline and the Topyo acid making reactor as byproduct steam; after the waste heat recovery pipeline exchanges heat through the heat recovery system, the gas in the pipe enters a Topusol acid making reactor; the heat energy recovery system recovers heat energy for other processes after the heat energy is used for byproduct steam.
Furthermore, the temperature of the flue gas at the outlet of the combustion furnace is 800-900 ℃ and the pressure is 0.05-0.2 MPa.
Further, the inlet of the combustion furnace is connected with a low-temperature methanol washing section, and H is absorbed by an absorption tower in the low-temperature methanol washing section2S is absorbed, forms sulfur-containing rich methanol with low-temperature methanol, is separated out in a sulfur-containing methanol flash tank, and is subjected to H2S concentration column to obtain 34% H2And S, entering a combustion furnace.
Further, the gas-liquid separator gas-phase outlet H2When the concentration of S is low, the sulfur is discharged after the environment is up to standard, and the sulfur enters a torch line and is sent to a torch, and the torch is ignited and combusted; h2When the concentration of S is high, the S is led to a waste heat recovery pipeline for recycling.
Compared with the prior art, the utility model discloses the beneficial effect who has does:
the utility model provides a conversion catalyst warming and vulcanizing system, which organically combines conversion vulcanization and Tuo ordinary process; one path of the outlet material of the combustion furnace enters a shift converter for vulcanization, nitrogen gas does not need to be supplemented and a new heat source does not need to be introduced in the vulcanization process, flue gas at the temperature of 850 ℃ in the combustion furnace is introduced, the use of an air separation device and a Roots machine is reduced, meanwhile, a new heat source does not need to be introduced in the shift catalyst vulcanization process, the cost is reduced, the corrosion of key equipment is reduced, the service life is prolonged, and the other path of the outlet material enters a Topuso acid-making reactor through a waste heat recovery pipeline for sulfur dioxide conversion; the flue gas introduced from the outlet of the combustion furnace in the acid making process of the Topusol is used for replacing 2.5MPa waste boiler heating gas in the temperature rising process, so that the vulcanization temperature is increased, the activity of a conversion catalyst is effectively activated, the CO index after conversion after the system is started is ensured, meanwhile, the weld crater cracking is effectively avoided, the times of parking and maintenance are reduced, the long-period stable operation of the system is ensured, and the problems of easy leakage of the 2.5MPa waste boiler and poor vulcanization effect of the catalyst are thoroughly solved.
Drawings
Fig. 1 is a schematic view of a shift catalyst temperature-rising vulcanizing system provided by the present invention.
In the figure: 1 is a shift converter, 2 is a water cooler, 3 is a gas-liquid separator, 4 is a combustion furnace, 5 is a Topusol acid-making reactor, and 6 is a heat energy recovery system.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
As shown in figure 1, a shift catalyst temperature-rising vulcanizing system comprises a shift converter 1, a water cooler 2, a gas-liquid separator 3, a combustion furnace 4, a Topyol acid-making reactor 5 and a heat energy recovery system 6; one path of the outlet of the combustion furnace 4 enters the shift converter 1 for shift catalyst vulcanization reaction, and the other path of the outlet enters the heat energy recovery system 6 through a waste heat recovery pipeline for heat recovery; one path of the outlet of the shift converter 1 enters a waste heat recovery pipeline, and the other path of the outlet enters a water cooler 2; the outlet of the water cooler 2 enters a gas-liquid separator 3; the gas phase of the gas-liquid separator 3 enters a waste heat recovery pipeline, and the liquid phase discharges sewage; the heat energy recovery system 6 uses the heat in the waste heat recovery pipeline and the Topyol acid making reactor 5 as byproduct steam; the gas in the waste heat recovery pipeline enters a Topusol acid making reactor 5 after heat exchange is carried out on the gas by a heat energy recovery system 6; the heat recovery system 6 recovers heat for use in other processes after the heat is used for the byproduct steam.
Furthermore, the temperature of the flue gas at the outlet of the combustion furnace 4 is 800-900 ℃ and the pressure is 0.05-0.2 MPa.
Further, the inlet of the combustion furnace 4 is connected with a low-temperature methanol washing section, and H is absorbed by an absorption tower in the low-temperature methanol washing section2S is absorbed, forms sulfur-containing rich methanol with low-temperature methanol, is separated out in a sulfur-containing methanol flash tank, and is subjected to H2S concentration column to obtain 34% H2S, enters the combustion furnace 4.
Further, the gas-liquid separator 3 has a gas-phase outlet H2When the concentration of S is low, the sulfur is discharged after the environment is up to standard, and the sulfur enters a torch line and is sent to a torch, and the torch is ignited and combusted; h2When the concentration of S is high, the S is led to a waste heat recovery pipeline for recycling.
In this embodiment, the inlet and outlet materials of each reactor are:
conversion furnace inlet material:
(1) flow rate: 167269Nm3H, wherein the CO is 20.443 percent and the H2:13.896%、CO211.766%, inert gas 0.059%, H2S:0.093%、COS:0.005%、H2O：53.5%
(2) Pressure: 3.8Mpa
(3) Temperature: 250 deg.C
Conversion furnace outlet material:
(1) flow rate: 167269Nm3H, wherein the CO is 3.822 percent and the H2:30.518%、CO228.387%, inert gas 0.059%, H2S:0.097%、COS:0.0007%、H2O：36.888%
(2) Pressure: 3.67Mpa
(3) Temperature: 412 deg.C
Combustion furnace inlet materials:
(1) flow rate: 651Nm of acidic gas3H, wherein CO2:56%、H2S:34%、N28 percent of carbon black; air: 1874Nm3/h wherein O2：21%、N2: 79 percent; mixed gas: 2525Nm3In which CO2:14.4%、H2S:8.7%、N2:60.6%、O2：15.5%
(2) Pressure: 0.1Mpa
(3) Temperature: 39 deg.C
Furnace exit material:
(1) flow rate: hot process gas 2414Nm3H, in which SO2:9.1%、CO2:15%、N2:63.5%、O2：2.5%、H2O：9.1%
(2) Pressure: 0.1Mpa
(3) Temperature: 850 deg.C
Import material of the Topusol acid making reactor:
(1) flow rate: thermal process gas 2664Nm3H, in which SO2:8.3%、CO2:13.6%、N2:64.9%、O2：4.3%、H2O：8.3%
(2) Pressure: 0.1Mpa
(3) Temperature: 420 deg.C
Outlet material of the Topusol acid-making reactor:
(1) flow rate: hot process gas 2553Nm3H, in which SO3:8.6%、CO2:14.2%、N2:67.7%、O2：0.1%、H2O：8.6%
(2) Pressure: 0.1Mpa
(3) Temperature: 383 deg.C
The above description has been made in detail only for the preferred embodiment of the present invention, but the present invention is not limited to the above embodiment, and various changes can be made without departing from the spirit of the present invention within the knowledge scope of those skilled in the art, and all such changes are intended to be encompassed by the present invention.
Claims (4)
1. A shift catalyst intensification vulcanization system which characterized in that: comprises a shift converter (1), a water cooler (2), a gas-liquid separator (3), a combustion furnace (4), a Topusol acid-making reactor (5) and a heat energy recovery system (6); one path of the outlet of the combustion furnace (4) enters a shift converter (1) for shift catalyst vulcanization reaction, and the other path of the outlet enters a heat energy recovery system (6) through a waste heat recovery pipeline for heat recovery; one path of an outlet of the shift converter (1) enters a waste heat recovery pipeline, and the other path of the outlet enters a water cooler (2); the outlet of the water cooler (2) enters a gas-liquid separator (3); the gas phase of the gas-liquid separator (3) enters a waste heat recovery pipeline, and the liquid phase discharges sewage; the heat recovery system (6) uses the heat in the waste heat recovery pipeline and the Topyol acid-making reactor (5) for by-product steam; the gas in the waste heat recovery pipeline enters a Topyol acid making reactor (5) after heat exchange of the waste heat recovery pipeline by a heat energy recovery system (6); the heat energy recovery system (6) recovers heat energy for the byproduct steam.
2. The shift catalyst temperature-rising vulcanization system according to claim 1, characterized in that: the temperature of the flue gas at the outlet of the combustion furnace (4) is 800-900 ℃, and the pressure is 0.05-0.2 MPa.
3. The shift catalyst temperature-increasing vulcanization system according to claim 1 or 2, characterized in that: the inlet of the combustion furnace (4) is connected with a low-temperature methanol washing working section, and H is absorbed by an absorption tower in the low-temperature methanol washing working section2S is absorbed, forms sulfur-containing rich methanol with low-temperature methanol, is separated out in a sulfur-containing methanol flash tank, and is subjected to H2S concentration column to obtain 34% H2S, entering a combustion furnace (4).
4. The shift catalyst temperature-rising vulcanization system according to claim 1, characterized in that: the gas-liquid separator (3) gas-phase outlet H2When the concentration of S is low, the sulfur is discharged after the environment is up to standard, and the sulfur enters a torch line and is sent to a torch, and the torch is ignited and combusted; h2When the concentration of S is high, the S is led to a waste heat recovery pipeline for recycling.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921306908.XU CN210675125U (en) | 2019-08-13 | 2019-08-13 | Shift catalyst intensification vulcanization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921306908.XU CN210675125U (en) | 2019-08-13 | 2019-08-13 | Shift catalyst intensification vulcanization system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210675125U true CN210675125U (en) | 2020-06-05 |
Family
ID=70890811
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921306908.XU Active CN210675125U (en) | 2019-08-13 | 2019-08-13 | Shift catalyst intensification vulcanization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210675125U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110327849A (en) * | 2019-08-13 | 2019-10-15 | 阳煤丰喜肥业（集团）有限责任公司 | A kind of transformation catalyst elevated temperature cure system |
-
2019
- 2019-08-13 CN CN201921306908.XU patent/CN210675125U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110327849A (en) * | 2019-08-13 | 2019-10-15 | 阳煤丰喜肥业（集团）有限责任公司 | A kind of transformation catalyst elevated temperature cure system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100544807C (en) | The method of a kind of sulphur recovery and exhaust gas processing device and sulphur recovery thereof and vent gas treatment | |
| CN105521687B (en) | A method of utilizing coal tar hydrogenating hydrogen sulfide gas by-product sulphur | |
| CN107777663B (en) | A kind of coupling process of lighter hydrocarbons hydrogen manufacturing and hydrogen from methyl alcohol | |
| CN101693164A (en) | Method for obtaining high-purity sulphur from Claus reactive tail-gases | |
| WO2023202139A1 (en) | System and method for hydrogen and power cogeneration of coal-fired boiler | |
| CN106621809A (en) | Regeneration tower waste heat recovering system and method of activated coke dry method desulfurizer | |
| CN210675125U (en) | Shift catalyst intensification vulcanization system | |
| CN201031142Y (en) | Sulfur recovery and exhaust gas treating device of reheat furnace hydrogen making | |
| CN101565172A (en) | Method for recovering sulfur from byproduct of acid gas generated in production of rubber chemicals | |
| CN216445007U (en) | High-temperature raw gas non-catalytic partial oxidation direct reforming system | |
| CN113955718B (en) | Direct reforming process and system for non-catalytic partial oxidation of high-temperature raw gas | |
| CN216192066U (en) | System for replacing crude benzene zone tube furnace with waste heat of coke oven flue gas waste heat boiler and ascending tube | |
| CN106397121A (en) | A biogas-coke oven gas combined methanol production device | |
| CN116081570A (en) | Natural gas reformer of flue gas recovery heat transfer | |
| CN104524970B (en) | A kind of selexol process exhaust gas purification system taking low-quality waste heat source as power | |
| CN104058368A (en) | Process and system for producing hydrogen by converting hydrocarbon-containing tail gas | |
| CN210150715U (en) | Natural gas steam reforming hydrogen production device | |
| CN204380511U (en) | A kind of selexol process exhaust gas purification system that is power with low-quality waste heat source | |
| CN209204977U (en) | A kind of sulfur recovery tail gas secondary desulfuration device | |
| CN213453572U (en) | Sulfur recovery unit waste heat utilization system | |
| CN203998947U (en) | A kind of hydrocarbonaceous tail gas reforming hydrogen manufacturing system | |
| CN215906138U (en) | System for replacing crude benzene zone tube furnace with superheated steam of coke dry quenching boiler of coke-oven plant | |
| CN211078472U (en) | Device for improving sulfur recovery efficiency | |
| CN215479716U (en) | Condensing hydrogen production converter system with tail gas and flue gas CCUS | |
| CN203545674U (en) | Methanol synthesis system with two reforming furnaces |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |