CN114515509A - Shutdown desulfurization device and desulfurization method for sulfur recovery system - Google Patents

Shutdown desulfurization device and desulfurization method for sulfur recovery system Download PDF

Info

Publication number
CN114515509A
CN114515509A CN202011303959.4A CN202011303959A CN114515509A CN 114515509 A CN114515509 A CN 114515509A CN 202011303959 A CN202011303959 A CN 202011303959A CN 114515509 A CN114515509 A CN 114515509A
Authority
CN
China
Prior art keywords
sulfur
tail gas
steam
gas
condenser
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.)
Granted
Application number
CN202011303959.4A
Other languages
Chinese (zh)
Other versions
CN114515509B (en
Inventor
瞿杨
傅适
雷婧
杨波
唐忠渝
涂婷娟
贾勇
许佳乐
徐飞
梁革
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Petrochina Co Ltd
Original Assignee
Petrochina Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Petrochina Co Ltd filed Critical Petrochina Co Ltd
Priority to CN202011303959.4A priority Critical patent/CN114515509B/en
Publication of CN114515509A publication Critical patent/CN114515509A/en
Application granted granted Critical
Publication of CN114515509B publication Critical patent/CN114515509B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/88—Handling or mounting catalysts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • B01D53/8609—Sulfur oxides
    • 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
    • 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

Abstract

The embodiment of the invention discloses a shutdown desulfurization device and a desulfurization method for a sulfur recovery system, and relates to the field of petrochemical industry. In the shutdown sulfur removal device, a main combustion furnace, a waste heat boiler, a primary Claus reactor, a secondary condenser, a secondary reheating furnace, a secondary Claus reactor, a tertiary condenser and a tail gas catcher are sequentially communicated through pipelines; the top outlet of the tail gas catcher is divided into a first branch and a second branch, the first branch is connected with the inlet end of the steam ejector, and the second branch is connected with the tail gas treatment unit; the outlet end of the steam injector is connected with the main combustion furnace; the second-stage condenser, the third-stage condenser and the tail gas catcher are respectively connected with the liquid sulfur pool. The sulfur removal method and the sulfur removal device provided by the embodiment of the invention can effectively reduce sulfur removal SO during the shutdown period of the sulfur recovery system2Concentration ofThe fluctuation range improves the desulfurization efficiency of the catalyst bed layer and shortens the shutdown time of the sulfur recovery system.

Description

Shutdown desulfurization device and desulfurization method for sulfur recovery system
Technical Field
The embodiment of the invention relates to the technical field of sulfur recovery, in particular to a shutdown sulfur removal device and a sulfur removal method for a sulfur recovery system.
Background
In a sulfur recovery device of a natural gas purification plant or a refinery plant, in particular a low-temperature Claus sulfur recovery device, elemental sulfur and a small amount of FeS attached to the gap of a catalyst bed layer of a Claus reactor need to be removed before shutdown or overhaul.
Among the correlation technique, for the flow that increases the process gas of whole sulphur removal in-process, main combustion furnace end at sulphur recovery unit adds partial nitrogen gas, adopt heating nitrogen gas to carry out the sulphur removal to sulphur recovery unit claus reactor catalyst bed, but the handling capacity of natural gas purification plant air nitrogen system is limited, in purification plant device shutdown in-process, desulphurization and dehydration device sweeps and also needs a large amount of nitrogen gas, lead to the required nitrogen gas volume of sulphur recovery unit can't satisfy the requirement through lasting with nitrogen gas increase process gas flow, lead to the sulphur removal rate lower.
Disclosure of Invention
The embodiment of the application provides a shutdown desulfurization device and a desulfurization method for a sulfur recovery system, so as to solve the problem that the desulfurization rate is low due to the fact that the nitrogen amount cannot meet the process gas flow in the related art.
The technical scheme is as follows:
in a first aspect, there is provided a shutdown sulphur removal unit for a sulphur recovery system, the shutdown sulphur removal unit comprising: the system comprises a main combustion furnace, a waste heat boiler, a primary Claus reactor, a secondary condenser, a secondary reheating furnace, a secondary Claus reactor, a tertiary condenser, a tail gas catcher, a liquid sulfur pool, a steam ejector and a tail gas treatment unit;
the main combustion furnace, the waste heat boiler, the primary Claus reactor, the secondary condenser, the secondary reheating furnace, the secondary Claus reactor, the tertiary condenser and the tail gas catcher are communicated in sequence through pipelines;
the top outlet of the tail gas catcher is divided into a first branch and a second branch, the first branch is connected with the inlet end of the steam ejector, and the second branch is connected with the tail gas treatment unit;
the outlet end of the steam injector is connected with the main combustion furnace;
the second-stage condenser, the third-stage condenser and the tail gas catcher are respectively connected with the liquid sulfur pool.
Optionally, the primary combustion furnace comprises a fuel gas inlet for admitting fuel gas into the primary combustion furnace, an air inlet for admitting air into the primary combustion furnace, and a temperature-regulated steam inlet;
the outlet end of the steam ejector is connected with the temperature-adjusting steam inlet.
Optionally, the exhaust trap comprises: a top outlet and a first liquid sulfur outlet;
the secondary condenser comprises a second liquid sulfur outlet;
the third-stage condenser comprises a third liquid sulfur outlet;
and a second liquid sulfur outlet of the secondary condenser, a third liquid sulfur outlet of the tertiary condenser and a first liquid sulfur outlet of the tail gas catcher are respectively connected with the liquid sulfur pool.
Optionally, a primary condenser and a primary reheating furnace are arranged between the waste heat boiler and the primary claus reactor, the primary condenser comprises a fourth liquid sulfur outlet, and the fourth liquid sulfur outlet is connected with the liquid sulfur pool.
Optionally, an ejector outlet flow regulating valve is arranged at the outlet end of the steam ejector, the outlet end of the steam ejector is divided into two paths after passing through the ejector outlet flow regulating valve, one path is connected with the temperature-regulating steam inlet through a circulating pipeline, and the other path is connected with the tail gas treatment unit through an emptying valve.
Optionally, the shutdown sulfur removal unit further comprises a pressure regulating valve disposed on the second branch.
In a second aspect, there is provided a process for removing sulfur using the shut down sulfur removal unit described above, the process comprising:
heating and mixing fuel gas, air, nitrogen and circulating tail gas in a main combustion furnace to form process gas;
the process gas is cooled by a waste heat boiler, enters a first-stage Claus reactor, elemental sulfur in a catalyst bed layer of the first-stage Claus reactor is vaporized, the elemental sulfur forms elemental sulfur steam, the elemental sulfur steam and the process gas enter a second-stage condenser for cooling, the elemental sulfur steam is condensed and separated into liquid sulfur and enters a liquid sulfur pool, the cooled process gas enters a second-stage reheating furnace for heating, the heated process gas enters a second-stage Claus reactor, the elemental sulfur in the catalyst bed layer of the second-stage Claus reactor is vaporized to form elemental sulfur steam, the formed elemental sulfur steam and the process gas enter a third-stage condenser for cooling, the elemental sulfur steam is condensed and separated into liquid sulfur and enters the liquid sulfur pool, the cooled process gas and residual elemental sulfur steam which is not condensed and separated enter a tail gas catcher, and the tail gas catcher catches and separates the residual elemental sulfur steam to form liquid sulfur and enters the liquid sulfur pool, discharging the obtained tail gas from an outlet at the top of the tail gas catcher;
one part of the tail gas enters a steam ejector through a first branch, and enters the main combustion furnace after being pressurized by the steam ejector;
and the other part of the tail gas enters the tail gas treatment unit through a second branch.
Optionally, after a part of the tail gas is pressurized by the steam ejector, the part of the tail gas is used as circulating tail gas and enters the temperature-adjusting steam inlet through a circulating tail gas pipeline, the flow of the circulating tail gas is controlled by the flow regulating valve at the outlet of the ejector, and the circulating tail gas with the redundant flow is discharged by the emptying valve and then enters the tail gas treatment unit.
Optionally, the process gas is cooled to 280-320 ℃ by a waste heat boiler.
Optionally, the mass flow ratio of the fuel gas to the circulating tail gas is 2-4: 1; and/or
The pressure of the circulating tail gas is 20-40 kPa.
The beneficial effects brought by the technical scheme provided by the embodiment of the application at least comprise:
according to the shutdown desulfurization device and the desulfurization method for the sulfur recovery system, the circulating tail gas is returned to be heated and mixed with the fuel gas, the air and the nitrogen to serve as the process gas, so that the flow rate of the process gas is increased, the consumption of the nitrogen is reduced, and the consumption of the nitrogen is saved; the process gas vaporizes and removes the elemental sulfur in the catalyst bed, the formed elemental sulfur steam flows along with the process gas, the elemental sulfur steam is cooled and separated into liquid sulfur, the rest process gas is pressurized by a steam ejector and then returns to be used as circulating tail gas, the circulating recovery of the tail gas is realized, and the sulfur removal SO during the shutdown period of the sulfur recovery system can be effectively reduced2The concentration fluctuation range improves the desulfurization efficiency of the catalyst bed layer, shortens the shutdown time of the sulfur recovery system and has simple process flow; the sulfur recovery system that this application embodiment provided stops sulphur removal device for through at tail gas trap top exit linkage steam jet ejector for retrieve tail gas and return to main burning furnace, simple structure, with low costs, have wide application prospect.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings needed to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
FIG. 1 shows a schematic view of the shut-down sulphur removal unit of a sulphur recovery system according to an embodiment of the invention;
FIG. 2 shows a schematic view of the shutdown sulfur removal unit of another sulfur recovery system according to an embodiment of the present invention.
The reference numerals denote:
1-an air inlet;
2-a fuel gas inlet;
3-a nitrogen line;
4-acid gas pipeline;
5-a main fuel furnace;
6, a waste heat boiler;
7-first-stage condenser;
8-liquid sulfur pool;
9-a first air inlet;
10-a first fuel gas inlet;
11-primary reheating furnace;
12-a primary claus reactor;
13-a secondary condenser;
14-a second air inlet;
15-a second fuel gas inlet;
16-secondary reheating furnace;
17-a secondary claus reactor;
18-a three-stage condenser;
19-a tail gas trap;
20-a recycle off-gas line;
21-a steam ejector;
22-a tail gas treatment unit;
23-ejector outlet flow regulating valve;
24-a pressure regulating valve;
25-a vent valve;
26-temperature regulating steam inlet;
27-a first branch;
28-second branch.
Detailed Description
In order to make the objects, technical solutions and advantages of the present application more clear, embodiments of the present application will be described in further detail below.
In the normal production process of the Claus sulfur recovery device of the natural gas purification plant or the refinery, H in the normal process gas2S、SO2The Claus reaction is carried out to generate elemental sulfur which is mainly S8Form exists, partly, as the device operatesSulfur vapour can condense in the pore structure of the catalyst surface, in particular in low temperature claus sulfur recovery processes, in low temperature claus reactors, H in the process gas2S、SO2Elemental sulfur generated by low-temperature Claus reaction is deposited in a gap structure of the catalyst, the gap deposited elemental sulfur of the catalyst is regenerated through switching of a hot-state Claus reactor and a cold-state Claus reactor, and partial elemental sulfur is deposited in gaps of the catalyst under the conditions of incomplete regeneration and the like in the daily production operation process due to low load of a device, long-time operation abrasion of the catalyst and the like.
Meanwhile, H is increased along with the increase of the operation time of the sulfur recovery device2S、SO2The materials such as FeS and the like generated by the corrosion of the device pipeline are stored in the catalyst bed layer of the Claus reactor, the FeS has low ignition point and is easy to spontaneously combust to cause the elemental sulfur stored in the catalyst bed layer to combust to generate SO2Causing the tail gas to discharge SO2Increases the environmental risk, and simultaneously emits a large amount of heat in the combustion process, causes the deactivation of the catalyst, and can damage equipment such as a Claus reactor in serious cases.
Therefore, before the sulfur recovery device is shut down or overhauled, elemental sulfur and a small amount of FeS attached to the gaps of the catalyst bed layer of the Claus reactor need to be removed. In the shutdown stage of the sulfur recovery device, when elemental sulfur in the gaps of the catalyst bed is removed, in order to improve the sulfur removal rate and reduce the discharged SO of tail gas2The sulfur recovery system is shut down to remove sulfur, and the sulfur removal device and the sulfur removal method are needed to treat tail gas.
In the embodiment of the invention, during the normal operation of the sulfur recovery device, the air from the main fan and the acid gas from the desulfurization unit enter the main combustion furnace, and one third of H in the acid gas2S and O in air2Combustion to form SO2And release a large amount of heat, leaving two thirds of H in the acid gas2S and SO2The primary combustion furnace generates a Claus reaction to generate elemental sulfur, the generated elemental sulfur enters a waste heat boiler along with high-temperature process gas in the form of elemental sulfur steam, the elemental sulfur enters a primary condenser for further cooling after being cooled by the waste heat boiler, and the elemental sulfur steam is cooledCondensing and separating into liquid sulfur, degassing and storing in a liquid sulfur pool, heating in a first-stage reheating furnace to reach the reaction temperature requirement of the first-stage Claus reactor, providing heat with fuel gas and air via heat release, feeding the heated process gas into the first-stage Claus reactor, and collecting H from the process gas2S and SO2The catalyst bed layer of the first-level Claus reactor continuously generates the Claus reaction to generate elemental sulfur steam, the elemental sulfur steam enters the second-level condenser along with the process gas to be cooled, the elemental sulfur steam is condensed and separated into liquid sulfur to the liquid sulfur pool to be degassed and stored, the cooled process gas enters the second-level reheating furnace to be heated so as to meet the temperature requirement of the second-level Claus reactor, the heat of the second-level reheating furnace is provided by the combustion of fuel gas and air to release heat, the heated process gas enters the second-level Claus reactor, and H in the process gas2S and SO2The Claus reaction continues to occur on a catalyst bed layer of the second-stage Claus reactor to generate elemental sulfur steam, the elemental sulfur steam enters the third-stage condenser along with the process gas to be cooled, the elemental sulfur steam is condensed and separated into liquid sulfur to be degassed and stored in the liquid sulfur pool, the cooled process gas enters the tail gas catcher, the tail gas catcher carries out catching and separation on residual elemental sulfur steam in the process gas, the liquid sulfur separated by catching and storage in the liquid sulfur pool is degassed, and the process gas after catching and separation enters a tail gas treatment unit, such as a tail gas treatment device or a tail gas incinerator.
In one aspect, the present invention provides a shutdown sulfur removal device for a sulfur recovery system, as shown in fig. 1 and 2, the sulfur removal device comprising: the system comprises a main combustion furnace 5, a waste heat boiler 6, a primary Claus reactor 12, a secondary condenser 13, a secondary reheating furnace 16, a secondary Claus reactor 17, a tertiary condenser 18, a tail gas catcher 19, a liquid sulfur pool 8, a steam ejector 21 and a tail gas treatment unit 22;
the main combustion furnace 5, the waste heat boiler 6, the primary Claus reactor 12, the secondary condenser 13, the secondary reheating furnace 16, the secondary Claus reactor 17, the tertiary condenser 18 and the tail gas catcher 19 are communicated in sequence through pipelines;
the top outlet of the tail gas catcher 19 is divided into a first branch 27 and a second branch 28, the first branch 27 is connected with the inlet end of the steam ejector 21, and the second branch 28 is connected with the tail gas treatment unit 22;
the outlet end of the steam injector 21 is connected with the main combustion furnace 5;
the two-stage condenser 13, the three-stage condenser 18 and the tail gas catcher 19 are respectively connected with the liquid sulfur pool 8, as shown in fig. 2.
According to the shutdown sulfur removal device provided by the embodiment of the invention, the steam ejector 21 is connected to the first branch 27 at the top outlet of the tail gas catcher 19, and the outlet end of the steam ejector 21 is connected with the main combustion furnace 5, so that the tail gas discharged by the tail gas catcher 19 is returned to the main combustion furnace 5 as the circulating tail gas, the flow rate of the process gas is increased, the consumption of the nitrogen gas is reduced, and the cyclic utilization of the tail gas is realized.
Optionally, the tail gas treatment unit 22 is used for treating tail gas entering the tail gas treatment unit 22, and the tail gas treatment unit 22 is a tail gas treatment device or an incinerator.
According to an embodiment of the present invention, the primary combustion furnace 5 comprises a fuel gas inlet 2, an air inlet 1 and a temperature-adjusting steam inlet 26, the fuel gas inlet 2 is used for allowing fuel gas to enter the primary combustion furnace 5, and the air inlet 1 is used for allowing air to enter the primary combustion furnace 5; the outlet end of the steam injector 21 is connected to a tempering steam inlet 26.
Optionally, the nitrogen gas line 5 and the acid gas line 4 are both connected to a temperature-regulating steam inlet 26, so that nitrogen gas enters the main combustion furnace 5 through the nitrogen gas line 5 from the temperature-regulating steam inlet 26.
Fuel gas and air respectively enter the combustion furnace 5 through the fuel gas inlet 2 and the air inlet 1, so that heat is provided in the combustion furnace 5 by heating, and circulating tail gas and nitrogen can enter the main combustion furnace 5 through the temperature-adjusting steam inlet 26, so that the fuel gas, the air, the nitrogen and the circulating tail gas are heated and mixed in the main combustion furnace 5 to form process gas for vaporizing and removing elemental sulfur deposited in catalyst beds of various stages of Claus reactors.
Optionally, the exhaust trap 19 comprises: a top outlet and a first liquid sulfur outlet; the second-stage condenser 13 comprises a second liquid sulfur outlet, the third-stage condenser 18 comprises a third liquid sulfur outlet, and the second liquid sulfur outlet of the second-stage condenser 13, the third liquid sulfur outlet of the third-stage condenser 18 and the first liquid sulfur outlet of the tail gas catcher 19 are respectively connected with the liquid sulfur pool 8.
The tail gas trap 19 is used for trapping gas entering the tail gas trap, for example, processing the process gas and the residual elemental sulfur vapor, so that the residual elemental sulfur vapor is condensed and separated into liquid sulfur, and the liquid sulfur is degassed and stored in the liquid sulfur pool 8, and the secondary condenser 13 and the tertiary condenser 18 can condense and separate the entering elemental sulfur vapor, so that the liquid sulfur is degassed and stored in the liquid sulfur pool 8.
Alternatively, a primary condenser 7 and a primary reheating furnace 11 are connected between the exhaust heat boiler 6 and the primary claus reactor 12, that is, the sulfur removal device includes a main combustion furnace 5, the exhaust heat boiler 6, the primary condenser 7, the primary reheating furnace 11, the primary claus reactor 12, a secondary condenser 13, a secondary reheating furnace 16, a secondary claus reactor 17, a tertiary condenser 18, and a tail gas trap 19, which are connected in this order, as shown in fig. 1.
The waste heat boiler 6 is used for cooling the process gas entering the waste heat boiler, the cooled process gas can enter the primary condenser 7 for further cooling, the process gas after further cooling enters the primary reheating furnace 11 for heating, and the primary condenser 7 can condense and separate the elemental sulfur steam flowing along with the process gas (including the circulating tail gas) into liquid sulfur to the liquid sulfur pool, so that the sulfur removal is further realized.
In an optional embodiment, after the elemental sulfur vapor enters the first-stage condenser 7, the second-stage condenser 13 and the third-stage condenser 18 along with the process gas, liquid sulfur in the elemental sulfur vapor is cooled and separated, the separated liquid sulfur respectively enters the liquid sulfur seals, the liquid sulfur flows into the degassing pool through the liquid sulfur seals, and H in the liquid sulfur is removed2And S, entering a liquid sulfur pool 8, and optionally, delivering the liquid sulfur to a sulfur forming unit through a liquid sulfur pump for preparing sulfur.
According to the embodiment of the invention, the outlet end of the steam ejector 21 is provided with an ejector outlet flow regulating valve 23, the outlet end of the steam ejector 21 is divided into two paths after passing through the ejector outlet flow regulating valve 23, one path is connected with a temperature regulating steam inlet 26 through a circulating pipeline 20, and the other path is connected with a tail gas treatment unit 22 through an emptying valve 25.
The steam ejector 21 is used for pressurizing the tail gas entering the steam ejector, the pressurized tail gas is returned to the main combustion furnace 5 as the circulating tail gas for increasing the process gas flow, and also can be used as temperature adjusting steam for reducing the temperature of the main combustion furnace 5, in the process that the circulating tail gas returns to the main combustion furnace 5 through the circulating pipeline 20, the flow of the circulating tail gas returning to the main combustion furnace 5 is controlled by the ejector outlet flow adjusting valve 23, and the circulating tail gas with the redundant flow is discharged to the tail gas treatment unit 22 through the emptying valve 25.
According to the shutdown desulfurization device for the sulfur recovery system, provided by the embodiment of the invention, the steam ejector 21 is connected to the top outlet of the tail gas catcher 19, so that the tail gas discharged from the top outlet of the tail gas catcher 19 is pressurized and returned to the main combustion furnace 5, the flow of the process gas is increased, the consumption of nitrogen is reduced, the desulfurization efficiency is improved, and the shutdown time of the sulfur recovery system is shortened.
Another aspect of an embodiment of the present invention provides a shutdown desulfurization method for a sulfur recovery system, the method comprising:
step 1, heating and mixing fuel gas, air, nitrogen and circulating tail gas to form process gas.
In the embodiment of the invention, air, fuel gas, nitrogen and circulating tail gas are heated and mixed in the main combustion furnace 5 to form high-temperature inert flue gas, namely process gas.
Wherein, the air is exported by the main fan export and is got into main combustion furnace 5 through air inlet 1 in, the fuel gas is the fuel gas of start-stop, and the fuel gas gets into main combustion furnace 5 through fuel gas entry 2 in, and nitrogen gas gets into main combustion furnace 5 through temperature regulating steam inlet 26 by air nitrogen system through nitrogen gas pipeline 3, and circulation tail gas is provided by steam jet ejector 21, and nitrogen gas and circulation tail gas get into main combustion furnace 5 through temperature regulating steam inlet 26.
In the embodiment of the invention, the fuel gas is combusted and heated in the main combustion furnace 5, the equivalent combustion of the fuel gas and the air can emit a large amount of heat, and the main combustion furnace 5 is made of metal, so that the main combustion furnace 5 can be damaged due to too high temperature (for example, over 1200 ℃), therefore, in order to protect the main combustion furnace 5, the circulating tail gas is introduced into the main combustion furnace 5 to replace the temperature-adjusting steam to protect the main combustion furnace 5, and the temperature of the main combustion furnace is reduced.
Meanwhile, nitrogen as inert gas does not react with sulfur, ferrous sulfide, sulfur steam and other substances in the Claus system, and the air nitrogen system adds nitrogen into the main combustion furnace 5 through the nitrogen pipeline 3 under the condition of meeting the nitrogen requirement, so that the flow and heat of the whole sulfur removal process can be increased.
In the embodiment of the invention, air, fuel gas, nitrogen and circulating tail gas enter the main combustion furnace 5 to be mixed, and high-temperature inert flue gas, namely process gas, is formed by combustion and heating of the fuel gas.
When the sulfur recovery system stops to remove sulfur, the boundary valve on the acid gas pipeline 4 needs to be closed, the acid gas is stopped from entering the main combustion furnace 5, and the fuel gas interlocking valve is opened, so that the fuel gas enters the main combustion furnace 5, and the switching of the fuel gas and the acid gas is completed.
Optionally, in step 1, the volume flow ratio of air to fuel gas in the primary fuel furnace 5 is (9-10): 1, for example, 9.8: 1.
Optionally, in step 1, the temperature of the main combustion furnace 5 is controlled to 1050-1150 ℃, for example 1100 ℃.
In order to avoid the formation of high temperature in the main combustion furnace 5 and protect and control the main combustion furnace 5, the weight flow ratio of the circulating tail gas to the fuel gas is (2-4): 1, wherein the density of the fuel gas is 0.717kg/m3. The flow rate of nitrogen gas is not particularly limited and is determined according to the amount of nitrogen gas that can be supplied in actual circumstances.
Optionally, in the step 1, the pressure of the fuel gas is 0.3 to 0.5MPa, for example, 0.4 MPa; the nitrogen pressure is 0.5 to 0.7MPa, for example 0.6 MPa; the air pressure is 80-90 kPa, such as 80 kPa; the steam ejector 21 pressurizes the circulating off gas to 20 to 40kPa, for example, 30kPa, and returns the pressurized gas to the main combustion furnace 5.
Step 2, the process gas is cooled by a waste heat boiler 6, enters a first-stage Claus reactor 12, elemental sulfur in a catalyst bed layer of the first-stage Claus reactor 12 is vaporized, the elemental sulfur forms elemental sulfur steam, the elemental sulfur steam and the process gas enter a second-stage condenser 13 for cooling, the elemental sulfur steam is condensed and separated into liquid sulfur and enters a liquid sulfur pool 8, the cooled process gas enters a second-stage reheating furnace 16 for heating, the heated process gas enters a second-stage Claus reactor 17, the elemental sulfur in the catalyst bed layer of the second-stage Claus reactor 17 is vaporized to form elemental sulfur steam, the formed elemental sulfur steam and the process gas enter a third-stage condenser 18 for cooling, the elemental sulfur steam is condensed and separated into liquid sulfur and enters the liquid sulfur pool 8, the cooled process gas and residual elemental sulfur steam which is not condensed and separated enter a tail gas catcher 19, the tail gas catcher 19 catches and separates the residual elemental sulfur vapor to form liquid sulfur, the liquid sulfur is sent to the liquid sulfur pool 8, and the obtained tail gas is discharged from the top outlet of the tail gas catcher 19.
In one embodiment, in step 2, the process gas enters the exhaust-heat boiler 6 from the main combustion furnace 5, is cooled by the exhaust-heat boiler 6, and then enters the primary claus reactor 12, so as to vaporize the elemental sulfur deposited in the gaps of the catalyst bed in the primary claus reactor 12, and the elemental sulfur forms elemental sulfur vapor.
Optionally, the process gas is cooled to 280-320 ℃ by the waste heat boiler 6, for example to 300 ℃.
In another embodiment, in step 2, the process gas enters the exhaust-heat boiler 6 from the main combustion furnace 5, is cooled by the exhaust-heat boiler 6, is cooled by the primary condenser 7, is heated by the primary reheating furnace 11, and then enters the primary claus reactor 12 to vaporize the elemental sulfur in the catalyst bed of the primary claus reactor 12, i.e., the elemental sulfur in the gaps of the catalyst bed is removed by vaporization, so as to form elemental sulfur vapor.
Optionally, cooling to 165-175 ℃, for example 170 ℃ by a primary condenser 7.
In the embodiment of the present invention, the primary condenser 7 may cool the residual elemental sulfur vapor (e.g., residual elemental sulfur vapor in the circulating tail gas) flowing along with the process gas, and the residual elemental sulfur vapor is cooled and separated into liquid sulfur, which enters the liquid sulfur pool 8 through the fourth liquid sulfur outlet.
Optionally, the mixture is heated to 280-320 ℃ by a primary reheating furnace 11, for example, 300 ℃. The process gas at 280-320 ℃ (such as 300 ℃) enters a first-stage Claus reactor 12, and elemental sulfur deposited in gaps in a catalyst bed layer in the first-stage Claus reactor can be vaporized and removed to form elemental sulfur steam.
Optionally, fuel gas and air are introduced into the primary reheating furnace 11 for heating so as to provide heat, the fuel gas enters the primary reheating furnace 11 from the first fuel gas inlet 10, the air enters the primary reheating furnace 11 from the first air inlet 9, and the volume flow ratio of the introduced fuel gas to the introduced air is 1 (9-10), for example, 1: 9.8.
The elemental sulfur vapor formed in the primary claus reactor 12 flows with the process gas.
Elemental sulfur vapor formed in the primary claus reactor 12 is cooled by the secondary condenser 13 along with the process gas, heated by the secondary reheating furnace 16, and then enters the secondary claus reactor 17 to vaporize and remove elemental sulfur in the catalyst bed of the secondary claus reactor 17, thereby forming elemental sulfur vapor, and the elemental sulfur vapor formed in the secondary claus reactor 17 flows along with the process gas.
Optionally, fuel gas and air are introduced into the secondary reheating furnace 16 for heating so as to provide heat, the fuel gas enters the secondary reheating furnace 16 from the second fuel gas inlet 15, the air enters the secondary reheating furnace 16 from the second air inlet 14, and the volume flow ratio of the introduced fuel gas to the introduced air is 1 (9-10), for example, 1: 9.8.
Optionally, the elemental sulfur vapor enters the secondary condenser 13 along with the process gas to be cooled to 165-175 ℃, for example, 170 ℃, in the secondary condenser 13, the elemental sulfur vapor is condensed into liquid sulfur, the liquid sulfur enters the liquid sulfur pool 8 from a second liquid sulfur outlet of the secondary condenser 13 to be degassed and stored, the cooled process gas enters the secondary reheating furnace 16 to be heated to 280-320 ℃, for example, 300 ℃, the heated process gas enters the secondary claus reactor 17 to vaporize and remove the elemental sulfur deposited in the gap of the catalyst bed in the secondary claus reactor 17 to form elemental sulfur vapor, and the elemental sulfur vapor formed in the secondary claus reactor 17 flows along with the process gas.
Elemental sulfur vapor formed in the second-stage Claus reactor 17 enters a third-stage condenser 18 along with the process gas, liquid sulfur separated from the elemental sulfur vapor by the third-stage condenser 18 enters a liquid sulfur pool 8 from a third liquid sulfur outlet for degassing and storage, and the cooled process gas enters a tail gas trap 19.
Optionally, the process gas and the elemental sulfur vapor are cooled to 165-175 ℃ by the three-stage condenser 18, for example, 170 ℃, the cooled process gas enters the tail gas trap 19, the tail gas trap 19 traps and separates residual elemental sulfur vapor flowing along with the process gas, the residual elemental sulfur vapor is trapped and separated into liquid sulfur, the liquid sulfur enters the liquid sulfur pool 8 from the first liquid sulfur outlet for degassing and storage, and the tail gas is discharged from the top outlet of the tail gas trap 19.
In the embodiment of the invention, the low-pressure saturated steam generated by the first-stage condenser 7, the second-stage condenser 13 and the third-stage condenser 18 can provide heat-preservation and heat-tracing steam for the sulfur removal device, and the rest steam can enter a low-pressure steam system pipe network of a whole plant after being regulated by the pressure regulating valve 24 to be used by other devices.
Step 3, enabling a part of the tail gas to enter a steam ejector through a first branch, and enabling the part of the tail gas to enter a main combustion furnace after being pressurized by the steam ejector; and the other part of the tail gas enters the tail gas treatment unit through a second branch.
In step 3, a part of the tail gas discharged from the top outlet of the tail gas catcher 19 enters the steam ejector 21 through the first branch 27, enters the main combustion furnace 5 after being pressurized by the steam ejector 21, and the other part of the tail gas enters the tail gas treatment unit 22 through the second branch 28.
Alternatively, the tail gas is pressurized by the steam ejector 21 and then enters the temperature-adjusting steam inlet 26 as a circulating tail gas through the circulating tail gas line 20 and returns to the main combustion furnace 5.
In the embodiment of the invention, a part of tail gas discharged from the top outlet of the tail gas catcher 19 enters the steam ejector 21 through the first branch 27, the steam ejector 21 boosts the process gas and returns to the temperature-adjusting steam inlet 26 of the main combustion furnace 5, so that the fuel gas, the air, the nitrogen and the circulating tail gas are heated and mixed in the main combustion furnace 5, the process gas flow and the heat of the whole sulfur removal device are increased, the nitrogen concentration in the process gas is increased, the formed high-temperature process gas sequentially enters the Claus reactors at all stages again to purge and remove sulfur from catalyst beds, and the problem that the catalyst beds are poor in air distribution is solvedElemental sulfur in the layer is combusted to increase SO in the system2Concentration, reducing the discharge of SO in tail gas2The concentration, the desulfurization efficiency and the heating rate of the catalyst bed layer are improved, and the desulfurization time of the catalyst bed layers of all stages of the Claus reactor is shortened, so that the shutdown time of a sulfur recovery system is saved.
During the shutdown period of the sulfur recovery system, the back pressure of the whole sulfur removal device is controlled by the pressure regulating valve 24, when the pressure is high, the pressure regulating valve 24 is opened, part of tail gas enters the tail gas treatment unit 22, such as a tail gas treatment device or an incinerator, through the pressure regulating valve 24, and when the pressure is low, the pressure regulating valve 24 is closed.
Optionally, the flow of the recycled tail gas is controlled by an ejector outlet flow regulating valve 23, and the surplus flow of the recycled tail gas is vented to the tail gas treatment unit 22 by a vent valve 25.
Alternatively, the sulfur removal process is ended when the amount of liquid sulfur flowing out of the bottom of the tail gas trap 19 is lower than a preset value.
Optionally, the sulphur removal process should be carried out for at least 24 hours, ensuring that no liquid sulphur flows to the bottom of the tail gas trap 19 to the liquid sulphur pool 8.
Optionally, the sulfur removal process further comprises: and (3) closing the primary reheating furnace 11 and the secondary reheating furnace 16, increasing the air quantity of the main combustion furnace 5, when the temperature of each point of the catalyst bed layer of each stage of the Claus reactor is reduced to 150-155 ℃, for example, about 150 ℃, shutting down the main combustion furnace 5, and closing the fuel gas inlet 2 and the temperature-adjusting steam inlet 26.
Optionally, when no liquid sulfur flows to the liquid sulfur pool 8 from the bottom of the tail gas catcher 19, the primary reheating furnace 11 and the secondary reheating furnace 16 are closed, the fuel gas of the primary combustion furnace 5 is continuously combusted, when the temperature of the catalyst bed layers in the primary claus reactor 12 and the secondary claus reactor 17 is reduced to 195-200 ℃, the air amount of the primary combustion furnace 5 is slowly increased, so that the excess oxygen content of the whole sulfur removal device is controlled to be 0.5-1%, when the air is excessive, the temperature of the catalyst bed layer is ensured to be below 230 ℃, if the temperature exceeds 230 ℃, the excess oxygen supply amount is reduced to stabilize or reduce the temperature of the catalyst bed layer, when the temperature of the catalyst bed layer is stable and tends to be, the air amount of the primary combustion furnace 5 is gradually increased, so that the excess oxygen content is gradually increased, when the temperature of the catalyst bed layer is reduced to about 150-155 ℃, the primary combustion furnace 5 is closed, the fuel gas inlet 2 and the temperature-adjusting combustion furnace steam inlet 26 are closed, the sulphur removal process is ended.
According to the shutdown desulfurization device and the desulfurization method for the sulfur recovery system, provided by the embodiment of the invention, the circulating tail gas is returned to be heated and mixed with the fuel gas, the air and the nitrogen to serve as the process gas, so that the flow rate of the process gas is increased, the consumption of the nitrogen is reduced, and the consumption of the nitrogen is saved; the process gas vaporizes and removes the elemental sulfur in the catalyst bed layer, the formed elemental sulfur steam flows along with the process gas and is cooled and separated into liquid sulfur, and the rest process gas is pressurized by a steam ejector and then returns to be used as circulating tail gas, SO that the circulating recovery of the tail gas is realized, and the sulfur removal SO during the shutdown of a sulfur recovery system can be effectively reduced2The concentration fluctuation range improves the desulfurization efficiency of the catalyst bed layer, shortens the shutdown time of the sulfur recovery system and has simple process flow; the shutdown desulphurization device for the sulfur recovery system, provided by the embodiment of the invention, has the advantages that the steam ejector is connected to the outlet at the top of the tail gas catcher, so that the circulating tail gas is returned to the main combustion furnace, the structure is simple, the cost is low, and the shutdown desulphurization device is suitable for the Claus sulfur recovery device corresponding to a natural gas purification plant or a refinery plant, such as a low-temperature Claus sulfur recovery device.
The following is illustrated in detail by way of example:
examples
There is provided a shutdown sulphur removal unit for a sulphur recovery system, the sulphur removal unit comprising: the system comprises a main combustion furnace, a waste heat boiler, a primary condenser, a primary reheating furnace, a primary Claus reactor, a secondary condenser, a secondary reheating furnace, a secondary Claus reactor, a tertiary condenser, a tail gas catcher, a liquid sulfur pool, a steam ejector and a tail gas processing unit;
the main combustion furnace, the waste heat boiler, the primary condenser, the primary reheating furnace, the primary Claus reactor, the secondary condenser, the secondary reheating furnace, the secondary Claus reactor, the tertiary condenser and the tail gas catcher are sequentially communicated through pipelines;
the top outlet of the tail gas catcher is divided into a first branch and a second branch, the first branch is connected with the inlet end of the steam ejector, the second branch is connected with the tail gas treatment unit, and the second branch is also provided with a pressure regulating valve; the outlet end of the steam injector is connected with a temperature-adjusting steam inlet of the main combustion furnace;
the first-stage condenser, the second-stage condenser, the third-stage condenser and the tail gas catcher are respectively connected with the liquid sulfur pool;
the outlet end of the steam ejector is provided with an ejector outlet flow regulating valve, the outlet end of the steam ejector is divided into two paths after passing through the ejector outlet flow regulating valve, one path is connected with the temperature-regulating steam inlet through a circulating pipeline, and the other path is connected with the tail gas treatment unit through an emptying valve.
Sulphur recovery system during normal production:
the air with the pressure of 90kPa from the main fan and the acid gas with the pressure of 90kPa from the desulfurization unit enter the main combustion furnace, and one third of H in the acid gas2S and O in air2Combustion to form SO2The reaction temperature is 1109 ℃, a great deal of heat is released, and two thirds of H are remained2S and SO formed2The method comprises the steps of generating a Claus reaction in a main combustion furnace to generate elemental sulfur, cooling the generated elemental sulfur to 316 ℃ along with high-temperature process gas through a waste heat boiler, enabling the cooled process gas to enter a primary condenser for further cooling to 170 ℃, condensing elemental sulfur vapor into separated liquid sulfur, degassing and storing the separated liquid sulfur in a liquid sulfur pool, heating the cooled process gas to 260 ℃ through a primary reheating furnace in order to meet the requirement of the reaction temperature of a primary Claus reactor, providing heat through combustion of fuel gas and air, enabling the heated process gas to enter a primary Claus reactor, and enabling H in the process gas to be generated2S and SO2The Claus reaction is continuously carried out on a catalyst bed layer of a first-stage Claus reactor to generate elemental sulfur steam, the temperature of process gas out of the first-stage Claus reactor is about 340 ℃, the process gas enters a second-stage condenser to be cooled to 170 ℃, the elemental sulfur steam is condensed into separated liquid sulfur, the separated liquid sulfur is sent to a liquid sulfur pool to be degassed and stored, the cooled process gas enters a second-stage reheating furnace to be heated to 220 ℃ so as to meet the requirement of the temperature of the second-stage Claus reactor, heat is provided by combustion of fuel gas and air, and the heated process gas enters a second-stage reheating furnace to be heatedFeeding into a secondary Claus reactor, and removing residual H in the process gas2S and SO2The catalyst bed layer of the second-stage Claus reactor continuously generates a Claus reaction to generate elemental sulfur vapor, the temperature of the process gas out of the second-stage Claus reactor is raised to 245 ℃, the process gas enters a third-stage condenser to be cooled to 170 ℃, the elemental sulfur vapor is condensed into separated liquid sulfur and is degassed and stored in a liquid sulfur pool, the cooled process gas and the cooled residual elemental sulfur vapor enter a tail gas catcher to catch and separate the residual sulfur vapor of the process gas, the residual sulfur vapor is caught and separated into liquid sulfur and is degassed and stored in the liquid sulfur pool, and the caught and separated process gas, namely the tail gas enters a tail gas treatment device or a tail gas incinerator.
Liquid sulfur condensed and separated by the first-stage condenser, the second-stage condenser and the third-stage condenser respectively enters the liquid sulfur seals, and the liquid sulfur which passes through the liquid sulfur seals at all stages automatically flows into a degassing pool to remove H in the liquid sulfur2And (5) after S, feeding the sulfur into a liquid sulfur pool, and then conveying the sulfur to a sulfur forming unit by using a liquid sulfur pump.
During the shutdown period of the sulfur recovery system:
the method comprises the steps of heating and mixing nitrogen with the pressure of 80kPa air from a main fan and the pressure of 0.6MPa from a start-stop fuel gas and nitrogen pipeline and circulating tail gas with the pressure of 30kPa from a circulating tail gas pipeline in a main combustion furnace to form inert high-temperature flue gas, namely process gas, wherein the volume flow ratio of the air to the fuel gas is 9.8:1, the weight ratio of the circulating tail gas to the fuel gas is 4:1, the nitrogen flow is determined according to actual conditions, the formed high-temperature process gas is cooled by a waste heat boiler to 300 ℃, the cooled process gas enters a primary condenser for further cooling to 170 ℃, is heated to 300 ℃ by an 11-stage reheating furnace, the heat is provided by the combustion heat release of the fuel gas and the air, the heated process gas enters a primary Claus reactor, the catalyst bed layer of the primary Claus reactor is heated by the high-temperature process gas, elemental sulfur in gaps is vaporized and removed, the formed elemental sulfur steam enters a secondary condenser along with process gas to be cooled to 170 ℃, the elemental sulfur steam is condensed and separated into liquid sulfur, the liquid sulfur is degassed and stored in a liquid sulfur pool, the cooled process gas enters a secondary reheating furnace to be heated to 300 ℃, heat is provided by combustion of fuel gas and air, the heated process gas enters a secondary Claus reactor, high-temperature process gas is used for vaporizing and removing the elemental sulfur in gaps of a catalyst bed layer of the secondary Claus reactor, the formed elemental sulfur steam enters the secondary condenser along with the process gas to be cooled to 170 ℃, the elemental sulfur steam is condensed into separated liquid sulfur, the separated liquid sulfur is degassed and stored in the liquid sulfur pool, the cooled process gas enters a tail gas catcher, and the tail gas catcher is used for catching and separating residual sulfur steam into liquid sulfur which is degassed and stored in the liquid sulfur pool.
The top outlet of the tail gas catcher discharges tail gas, the tail gas is pressurized by a steam ejector and then returns to the temperature-adjusting steam inlet of the main combustion furnace as circulating tail gas, the circulating tail gas is mixed with start-stop fuel gas, air and nitrogen in the main combustion furnace in a heating manner to form process gas, the flow and heat of the process gas of the whole sulfur removal device are increased, the nitrogen concentration in the process gas is increased, and the process gas with high temperature enters the reactor again to sweep and remove sulfur from the catalyst bed layer.
During the period, the back pressure of the whole system is controlled by the pressure regulating valve, the pressure regulating valve is opened when the pressure is high, partial tail gas enters the tail gas treatment device or the tail gas incinerator through the pressure regulating valve, and the pressure regulating valve is closed when the pressure is low.
The flow of the circulating tail gas is controlled by an ejector outlet flow regulating valve, and the circulating tail gas with redundant flow is discharged to a tail gas treatment device or a tail gas incinerator through a vent valve.
In the operation process of the sulfur removal device, when no liquid flow enters the liquid flow pool or the liquid sulfur amount is lower than a set value, the steam ejector closes the primary reheating furnace and the secondary reheating furnace, the combustion of fuel gas in the main combustion furnace is continuously maintained, and when the temperature of each point of a catalyst bed layer in each stage of Claus reactor is reduced to 195 ℃, the air amount of the main combustion furnace is slowly increased, so that the excess O in the system is increased2The content is controlled within 0.5-1%. When the temperature of catalyst bed layer of every stage of Claus reactor is stable and is in downward trend, the air quantity of main combustion furnace can be gradually increased so as to make excess O in the process gas2The content of the catalyst is gradually increased when the catalyst is catalyzed by a first-stage Claus reactor, a second-stage Claus reactor and a third-stage Claus reactorWhen the temperature of each point of the agent bed layer is reduced to about 150 ℃, the main combustion furnace is flamed out and stopped, fuel gas is stopped from entering the main combustion furnace, and the sulfur removal is finished.
In conclusion, the embodiment of the invention returns the circulating tail gas pressurized by the steam ejector to the main combustion furnace, increases the flow rate of the process gas, reduces the consumption of nitrogen, and reduces the sulfur removal SO during the shutdown period of the sulfur recovery system2The concentration fluctuation range improves the sulfur removal efficiency and shortens the shutdown time of the sulfur recovery system.
The above description is intended only to illustrate the alternative embodiments of the present application, and should not be construed as limiting the scope of the present application, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present application should be included in the scope of the present application.

Claims (10)

1. A shutdown sulphur removal unit for a sulphur recovery system, the shutdown sulphur removal unit comprising: the system comprises a main combustion furnace, a waste heat boiler, a primary Claus reactor, a secondary condenser, a secondary reheating furnace, a secondary Claus reactor, a tertiary condenser, a tail gas catcher, a liquid sulfur pool, a steam ejector and a tail gas treatment unit;
the main combustion furnace, the waste heat boiler, the primary Claus reactor, the secondary condenser, the secondary reheating furnace, the secondary Claus reactor, the tertiary condenser and the tail gas catcher are communicated in sequence through pipelines;
the top outlet of the tail gas catcher is divided into a first branch and a second branch, the first branch is connected with the inlet end of the steam ejector, and the second branch is connected with the tail gas treatment unit;
the outlet end of the steam injector is connected with the main combustion furnace;
the second-stage condenser, the third-stage condenser and the tail gas catcher are respectively connected with the liquid sulfur pool.
2. The shutdown sulfur removal unit of claim 1 wherein said primary combustion furnace comprises a fuel gas inlet for admitting fuel gas into said primary combustion furnace, an air inlet for admitting air into said primary combustion furnace, and a trim steam inlet;
the outlet end of the steam ejector is connected with the temperature-adjusting steam inlet.
3. The shutdown sulfur removal plant according to claim 1, wherein said tail gas trap comprises: a top outlet and a first liquid sulfur outlet;
the secondary condenser comprises a second liquid sulfur outlet;
the tertiary condenser comprises a third liquid sulfur outlet;
and a second liquid sulfur outlet of the secondary condenser, a third liquid sulfur outlet of the tertiary condenser and a first liquid sulfur outlet of the tail gas catcher are respectively connected with the liquid sulfur pool.
4. The shutdown sulfur removal device of claim 1, wherein a primary condenser and a primary reheating furnace are arranged between the waste heat boiler and the primary claus reactor, the primary condenser comprises a fourth liquid sulfur outlet, and the fourth liquid sulfur outlet is connected with the liquid sulfur pool.
5. The shutdown sulfur removal device according to any one of claims 2 to 4, wherein the outlet end of the steam ejector is provided with an ejector outlet flow regulating valve, the outlet end of the steam ejector is divided into two paths after passing through the ejector outlet flow regulating valve, one path is connected with the temperature-regulating steam inlet through a circulating pipeline, and the other path is connected with the tail gas treatment unit through a blow-down valve.
6. The shutdown sulfur removal unit of claim 1, further comprising a pressure regulating valve disposed on the second branch.
7. A shutdown sulphur removal process for a sulphur recovery system, the process being carried out using the shutdown sulphur removal unit of any one of claims 1 to 6, the process comprising:
heating and mixing fuel gas, air, nitrogen and circulating tail gas in a main combustion furnace to form process gas;
the process gas is cooled by a waste heat boiler, enters a first-stage Claus reactor, elemental sulfur in a catalyst bed layer of the first-stage Claus reactor is vaporized, the elemental sulfur forms elemental sulfur steam, the elemental sulfur steam and the process gas enter a second-stage condenser for cooling, the elemental sulfur steam is condensed and separated into liquid sulfur and enters a liquid sulfur pool, the cooled process gas enters a second-stage reheating furnace for heating, the heated process gas enters a second-stage Claus reactor, the elemental sulfur in the catalyst bed layer of the second-stage Claus reactor is vaporized to form elemental sulfur steam, the formed elemental sulfur steam and the process gas enter a third-stage condenser for cooling, the elemental sulfur steam is condensed and separated into liquid sulfur and enters the liquid sulfur pool, the cooled process gas and residual elemental sulfur steam which is not condensed and separated enter a tail gas catcher, the tail gas catcher catches and separates the residual elemental sulfur steam to form liquid sulfur and enters the liquid sulfur pool, discharging the obtained tail gas from an outlet at the top of the tail gas catcher;
a part of the tail gas enters a steam ejector through a first branch, and enters the main combustion furnace after being pressurized by the steam ejector;
and the other part of the tail gas enters the tail gas treatment unit through a second branch.
8. The shutdown sulfur removal method of claim 7, wherein a part of the tail gas is pressurized by the steam ejector and then enters the temperature-adjusting steam inlet as a circulating tail gas through a circulating tail gas pipeline, the flow rate of the circulating tail gas is controlled by the ejector outlet flow regulating valve, and the redundant flow rate of the circulating tail gas is vented by the vent valve and then enters the tail gas treatment unit.
9. The shutdown sulfur removal method of claim 7, wherein the process gas is cooled to 280-320 ℃ by the waste heat boiler.
10. The shutdown sulfur removal process of any one of claims 7 to 9, wherein the mass flow ratio of the fuel gas to the cycle tail gas is from 2 to 4: 1; and/or
The pressure of the circulating tail gas is 20-40 kPa.
CN202011303959.4A 2020-11-19 2020-11-19 Shutdown sulfur removal device and method for sulfur recovery system Active CN114515509B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202011303959.4A CN114515509B (en) 2020-11-19 2020-11-19 Shutdown sulfur removal device and method for sulfur recovery system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202011303959.4A CN114515509B (en) 2020-11-19 2020-11-19 Shutdown sulfur removal device and method for sulfur recovery system

Publications (2)

Publication Number Publication Date
CN114515509A true CN114515509A (en) 2022-05-20
CN114515509B CN114515509B (en) 2023-10-31

Family

ID=81594898

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202011303959.4A Active CN114515509B (en) 2020-11-19 2020-11-19 Shutdown sulfur removal device and method for sulfur recovery system

Country Status (1)

Country Link
CN (1) CN114515509B (en)

Citations (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0059548A1 (en) * 1981-03-02 1982-09-08 Standard Oil Company Method and apparatus for treating sulfur-containing gas stream
US4980146A (en) * 1985-10-25 1990-12-25 Societe Nationale Elf Aquitaine (Production) Process for removing sulphur compounds contained in a residual gas
CN1105175A (en) * 1993-03-16 1995-07-12 埃尔夫·阿奎坦生产公司 Method for removing sulphur compounds from a residual gas such as a residual gas from a claus process sulphur plant, and recovering said compounds as sulphur
CN101054165A (en) * 2007-01-30 2007-10-17 四川四维工程设计有限公司 Device and method of reclaim and processing tail gas of sulfur
CN103159187A (en) * 2013-03-27 2013-06-19 山东三维石化工程股份有限公司青岛分公司 Shutdown technique of cleaner production of sulfur recovery and tail gas treatment device
CN206437872U (en) * 2017-01-05 2017-08-25 中国石油化工股份有限公司 Hot nitrogen blows sulphur system
CN206447572U (en) * 2017-01-05 2017-08-29 中国石油化工股份有限公司 Hot nitrogen purges sulfur recovery facility
CN206521281U (en) * 2017-01-05 2017-09-26 中国石油化工股份有限公司 Novel sulphur reclaiming device
CN108557773A (en) * 2018-04-18 2018-09-21 陕西未来能源化工有限公司 A kind of Crouse's temperature control system and its method
CN108654337A (en) * 2018-04-18 2018-10-16 陕西未来能源化工有限公司 A kind of guard method of sulfur recovery system catalyst
CN209173684U (en) * 2018-10-24 2019-07-30 中国石油化工股份有限公司 Hot nitrogen purges sulphur unit
CN209651900U (en) * 2018-11-29 2019-11-19 中国石油天然气股份有限公司西南油气田分公司重庆天然气净化总厂 A kind of Crouse's sulfur recovery system
CN209652260U (en) * 2018-11-29 2019-11-19 中国石油天然气股份有限公司西南油气田分公司重庆天然气净化总厂 A kind of Crouse's sulphur recovery and exhaust treatment system
CN210973883U (en) * 2019-08-02 2020-07-10 中国石油化工股份有限公司 Sulfur recovery device is blown in circulation

Patent Citations (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0059548A1 (en) * 1981-03-02 1982-09-08 Standard Oil Company Method and apparatus for treating sulfur-containing gas stream
US4980146A (en) * 1985-10-25 1990-12-25 Societe Nationale Elf Aquitaine (Production) Process for removing sulphur compounds contained in a residual gas
CN1105175A (en) * 1993-03-16 1995-07-12 埃尔夫·阿奎坦生产公司 Method for removing sulphur compounds from a residual gas such as a residual gas from a claus process sulphur plant, and recovering said compounds as sulphur
CN101054165A (en) * 2007-01-30 2007-10-17 四川四维工程设计有限公司 Device and method of reclaim and processing tail gas of sulfur
CN103159187A (en) * 2013-03-27 2013-06-19 山东三维石化工程股份有限公司青岛分公司 Shutdown technique of cleaner production of sulfur recovery and tail gas treatment device
CN206437872U (en) * 2017-01-05 2017-08-25 中国石油化工股份有限公司 Hot nitrogen blows sulphur system
CN206447572U (en) * 2017-01-05 2017-08-29 中国石油化工股份有限公司 Hot nitrogen purges sulfur recovery facility
CN206521281U (en) * 2017-01-05 2017-09-26 中国石油化工股份有限公司 Novel sulphur reclaiming device
CN108557773A (en) * 2018-04-18 2018-09-21 陕西未来能源化工有限公司 A kind of Crouse's temperature control system and its method
CN108654337A (en) * 2018-04-18 2018-10-16 陕西未来能源化工有限公司 A kind of guard method of sulfur recovery system catalyst
CN209173684U (en) * 2018-10-24 2019-07-30 中国石油化工股份有限公司 Hot nitrogen purges sulphur unit
CN209651900U (en) * 2018-11-29 2019-11-19 中国石油天然气股份有限公司西南油气田分公司重庆天然气净化总厂 A kind of Crouse's sulfur recovery system
CN209652260U (en) * 2018-11-29 2019-11-19 中国石油天然气股份有限公司西南油气田分公司重庆天然气净化总厂 A kind of Crouse's sulphur recovery and exhaust treatment system
CN210973883U (en) * 2019-08-02 2020-07-10 中国石油化工股份有限公司 Sulfur recovery device is blown in circulation

Also Published As

Publication number Publication date
CN114515509B (en) 2023-10-31

Similar Documents

Publication Publication Date Title
US8080089B1 (en) Method and apparatus for efficient gas treating system
EP0190366B1 (en) Boiler capable of recovering waste heat and having denitration devices
CN101418246B (en) Low temperature methanol washing integrated Claus sulfur recovery system and process
CA3071602C (en) Acid gas removal apparatus and acid gas removal method
JP5766434B2 (en) Fluid catalytic cracking process with reduced carbon dioxide emissions
CN101899329A (en) Be used to handle the system and method for the stream that comprises undesirable emission gas
EP2307121A1 (en) Method and device for separating carbon dioxide from a waste gas of a fossil fuel-operated power plant
US20070215522A1 (en) Method for producing gas turbine fuel, and method and system for generating electric power by gas turbine
WO2008097839A1 (en) Methods and apparatus for removing acid gases from a natural gas stream
KR20070116010A (en) Method of operating a gas engine plant and fuel feeding system of a gas engine
CN104986740B (en) A kind of claus tail-gas clean-up system and processing method
CN103328774A (en) Method and system for energy generation in a chemical plant by utilizing flare gas
CN108298505A (en) Processing contains H2The process integration of S sour gas while extracting sulfuric acid and sulphur
CN110937648A (en) Process and device for continuously treating high-concentration organic wastewater
CN114515509A (en) Shutdown desulfurization device and desulfurization method for sulfur recovery system
JP2004345904A (en) Method and apparatus for recovering sulfur
EP1916024A1 (en) Unit and process for treating refinery process wastewater
CN115614188A (en) Marine liquid ammonia fuel supply system and fuel recovery system and method thereof
CN105480951A (en) Liquid sulfur degassing system and liquid sulfur degassing method
JP4135871B2 (en) Apparatus and method for reforming kerosene or light oil using exhaust heat as a heat source
EP2711334B1 (en) Method of production of pure hydrogen from a denatured hydrocarbon feedstock including a desulfurization stage with temperature control upstream the PSA
KR20210036175A (en) Integrated processing system for VOC in vessel
CN116672884B (en) Catalytic oxidation system and catalytic oxidation method for efficiently converting and removing VOCs in coal chemical industry
RU2791272C1 (en) Adsorption installation for natural gas preparation and transportation
CN115854336B (en) Method and device for mixing fuel of circulating fluidized bed boiler with fire-driving flue gas

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant