CN114074923B - Low-temperature sulfur recovery system and low-temperature sulfur recovery method - Google Patents

Low-temperature sulfur recovery system and low-temperature sulfur recovery method Download PDF

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Publication number
CN114074923B
CN114074923B CN202010817066.5A CN202010817066A CN114074923B CN 114074923 B CN114074923 B CN 114074923B CN 202010817066 A CN202010817066 A CN 202010817066A CN 114074923 B CN114074923 B CN 114074923B
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way valve
interface
condenser
reactor
cba
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CN114074923A (en
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张小兵
瞿杨
黄朝齐
傅适
王灵军
袁铖
何为
吴智晖
兰铃
邓苏恒
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Petrochina Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • 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
    • C01B17/0452—Process control; Start-up or cooling-down procedures of the Claus process
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

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  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Automation & Control Theory (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention discloses a low-temperature sulfur recovery system and a low-temperature sulfur recovery method, belonging to the field of low-temperature sulfur recovery, and comprising a low-temperature sulfur recovery system and a low-temperature sulfur recovery methodThe sulfur recovery system comprises an acid gas preheating treatment unit, a main reaction unit, a secondary reaction unit and a tail gas incineration unit which are connected in sequence. The secondary reaction unit includes: three CBA reactors and valve assemblies; the three CBA reactors are switched between a regeneration state and an adsorption state; the valve assembly is configured to position the regenerated CBA reactor between two adsorbed CBA reactors by switching the valve. By switching the valve, a great amount of hydrogen sulfide and sulfur dioxide gas contained in the regenerated CBA reactor and the catalyst pores does not directly enter the tail gas incineration unit any more, but enters the tail gas incineration unit after the Claus reaction of the adsorbed CBA reactor at the rear end of the regenerated CBA reactor. So arranged, H in the tail gas can be avoided 2 S and SO 2 Is beneficial to improving the recovery rate of sulfur at the same time.

Description

Low-temperature sulfur recovery system and low-temperature sulfur recovery method
Technical Field
The invention relates to the field of sulfur recovery, in particular to a low-temperature sulfur recovery system and a low-temperature sulfur recovery method.
Background
In petrochemical industry, coal chemical industry and other processes, H is usually generated 2 Acid gas with higher S content is generally treated by a sulfur recovery process, and H is treated by 2 S as much as possibleIs converted into elemental sulfur. A cold bed adsorption (Cold Bed Adsorption, abbreviated as CBA) unit is a low temperature claus sulfur recovery unit that converts hydrogen sulfide in sour gas to elemental sulfur through a thermal reaction furnace, a conventional claus reactor, and 3 CBA reactors.
When the CBA sulfur recovery device is used for sulfur recovery, when two CBA reactors are in the adsorption stage, the other CBA reactor is in the regeneration stage, and the operation of the three CBA reactors is switched, so that each CBA reactor is switched between the reaction stage and the regeneration stage.
In carrying out the invention, the present inventors have found that there are at least the following problems in the prior art:
during CBA reactor switching operations, there is a reactor that has just been completed that is moved to the end of the reactor sequence, such that a large amount of H 2 S and SO 2 Along with the direct discharge of the tail gas, the tail gas SO appears 2 The "spike" emission phenomenon, in which the emission rate rises rapidly, is detrimental to environmental safety.
Disclosure of Invention
In view of the above, the present invention provides a low-temperature sulfur recovery system and a low-temperature sulfur recovery method, which can solve the above-mentioned technical problems.
Specifically, the method comprises the following technical scheme:
in one aspect, a low temperature sulfur recovery system is provided, the low temperature sulfur recovery system comprising: the device comprises an acid gas preheating treatment unit, a main reaction unit, a secondary reaction unit and a tail gas incineration unit which are connected in sequence;
wherein the secondary reaction unit comprises: three CBA reactors and valve assemblies;
the three CBA reactors are switched between a regeneration state and an adsorption state;
the valve assembly is configured to position the regenerated CBA reactor between two adsorbed CBA reactors by switching the valve.
In some possible implementations, the main reaction unit includes: a claus reactor, a claus condenser;
the secondary reaction unit includes: the system comprises a first CBA reactor, a second CBA reactor, a third CBA reactor, a first condenser, a second condenser, a third condenser, a first three-way valve, a second three-way valve, a third three-way valve, a fourth three-way valve, a first two-way valve, a second two-way valve, a third two-way valve and a valve controller;
the outlet of the Claus reactor and the first interface of the first three-way valve are sequentially connected;
the outlet of the claus reactor, the claus condenser and the second interface of the first three-way valve are sequentially connected;
The third interface of the first three-way valve, the first two-way valve, the first CBA reactor, the first condenser and the first interface of the second three-way valve are sequentially connected;
the second interface of the second three-way valve is connected with the tail gas incineration unit, and the third interface of the second three-way valve, the second CBA reactor, the second condenser and the first interface of the third three-way valve are sequentially connected;
the second interface of the third three-way valve is connected with the tail gas incineration unit, and the third interface of the third three-way valve, the third CBA reactor, the third condenser and the first interface of the fourth three-way valve are sequentially connected;
the second interface of the fourth three-way valve is connected with the tail gas incineration unit, and the third interface of the fourth three-way valve and the inlet of the first CBA reactor are connected;
the second two-way valve is positioned on a connecting pipeline between a third interface of the first three-way valve and an inlet of the second CBA reactor;
the third two-way valve is positioned on a connecting pipeline between a third interface of the first three-way valve and an inlet of the third CBA reactor;
the valve controller is configured to control opening and closing operations of the first three-way valve, the second three-way valve, the third three-way valve, the fourth three-way valve, the first two-way valve, the second two-way valve, and the third two-way valve so that the regenerated CBA reactor is positioned between the two adsorbed CBA reactors.
In some possible implementations, the sour gas preheating treatment unit includes: the system comprises an acid-gas separator, an acid-gas preheater, a main fan, an air preheater, a main combustion furnace, a waste heat boiler, a front condenser and a reheater;
the acid gas separator, the acid gas preheater, the main combustion furnace, the waste heat boiler, the front condenser and the reheater are sequentially connected through pipelines;
the main fan, the air preheater and the main combustion furnace are sequentially connected through pipelines.
In some possible implementations, the tail gas incineration unit comprises: the tail gas catcher and the tail gas burning furnace are connected in sequence.
On the other hand, the embodiment of the invention also provides a low-temperature sulfur recovery method, which adopts any low-temperature sulfur recovery system.
In some possible implementations, the low temperature sulfur recovery method includes:
carrying out heat treatment on the acid gas to be treated by using an acid gas preheating treatment unit to obtain the acid gas to be treated with a set temperature;
carrying out a claus reaction on the acid gas to be treated with the set temperature in the main reaction unit to obtain a process gas;
carrying out claus reaction on the process gas in the secondary reaction unit to obtain tail gas, wherein the gas discharged from the regenerated CBA reactor enters an adsorbed final-stage CBA reactor;
And treating the tail gas by using the tail gas incineration unit to obtain exhaust gas.
In some possible implementations, the low temperature sulfur recovery method includes: the first interface of the first three-way valve is communicated with the third interface, the first interface of the second three-way valve and the third three-way valve are communicated with the third interface, the first interface of the fourth three-way valve is communicated with the second interface, the first two-way valve is opened, the second two-way valve and the third two-way valve are closed, at the moment, the process gas from the Claus reactor sequentially passes through the first CBA reactor, the first condenser, the second CBA reactor, the second condenser, the third CBA reactor and the third condenser until the first CBA reactor is completely regenerated, and at the same time, the second interface of the fourth three-way valve discharges tail gas to a tail gas incineration unit;
the valve controller is used for switching the first three-way valve, so that a second interface of the first three-way valve is communicated with a third interface, and the states of other valves are unchanged, at the moment, the process gas from the Claus reactor is cooled through the Claus condenser, and the cooled process gas sequentially passes through the first CBA reactor, the first condenser, the second CBA reactor, the second condenser, the third CBA reactor and the third condenser, and meanwhile, the second interface of the fourth three-way valve is used for discharging tail gas to a tail gas incineration unit;
Through the valve controller, the third three-way valve is switched, so that the first interface and the second interface of the third three-way valve are communicated, meanwhile, the third two-way valve is opened, the states of other valves are unchanged, at the moment, the process gas from the Claus reactor is cooled by the Claus condenser, and the cooled process gas is divided into two paths:
part of the cooled process gas passes through the third CBA reactor and the third condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a fourth three-way valve; the other part of the cooled process gas sequentially passes through the first CBA reactor, the first condenser, the second CBA reactor and the second condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a third three-way valve;
through the valve controller, switch the fourth three-way valve, make the first interface and the third interface intercommunication of fourth three-way valve, simultaneously close first two-way valve, the remaining valve state is unchangeable, and at this moment, the process gas from claus reactor is cooled by claus condenser, and the process gas after the cooling is in proper order through third CBA reactor third condenser first CBA reactor first condenser second CBA reactor second condenser simultaneously is discharged tail gas by the second interface of third three-way valve to tail gas incineration unit.
In some possible implementations, the low temperature sulfur recovery method further includes:
the first interface of the first three-way valve is communicated with the third interface, the first interfaces of the second three-way valve and the fourth three-way valve are communicated with the third interface, the first interface of the third three-way valve is communicated with the second interface, the third two-way valve is opened, the second two-way valve and the first two-way valve are closed, and at the moment, the process gas from the Claus reactor sequentially passes through the third CBA reactor, the third condenser, the first CBA reactor, the first condenser, the second CBA reactor and the second condenser until the third CBA reactor is completely regenerated, and at the same time, the tail gas is discharged to the tail gas incineration unit through the second interface of the third three-way valve;
the valve controller is used for switching the first three-way valve, so that a second interface of the first three-way valve is communicated with a third interface, and the states of other valves are unchanged, at the moment, the process gas from the Claus reactor is cooled through the Claus condenser, and the cooled process gas sequentially passes through the third CBA reactor, the third condenser, the first CBA reactor, the first condenser, the second CBA reactor and the second condenser, and meanwhile, the second interface of the third three-way valve is used for discharging tail gas to a tail gas incineration unit;
Through the valve controller, switch the second three-way valve, make the first interface and the second interface intercommunication of second three-way valve, simultaneously, open the second two-way valve, the remaining valve state is unchangeable, and at this moment, the process gas from claus reactor cools off through claus condenser, and the process gas after the cooling off carries out in two ways:
part of the cooled process gas passes through the second CBA reactor and the second condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a third three-way valve; the other part of the cooled process gas sequentially passes through the third CBA reactor, the third condenser, the first CBA reactor and the first condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a second three-way valve;
through the valve controller, switch the third three-way valve, make the first interface and the third interface intercommunication of third three-way valve, simultaneously close the third two-way valve, the remaining valve state is unchangeable, and at this moment, the process gas from claus reactor is cooled by claus condenser, and the process gas after the cooling is in proper order through the second CBA reactor second condenser third CBA reactor third condenser first CBA reactor first condenser, exhaust gas is discharged to tail gas incineration unit by the second interface of second three-way valve simultaneously.
In some possible implementations, the low temperature sulfur recovery method further includes:
the first interface of the first three-way valve is communicated with the third interface through the valve controller, the first interfaces of the third three-way valve and the fourth three-way valve are communicated with the third interface, the first interface of the first three-way valve is communicated with the second interface, the second two-way valve is opened, the third two-way valve and the first two-way valve are closed, and at the moment, the process gas from the Claus reactor sequentially passes through the second CBA reactor, the second condenser, the third CBA reactor, the third condenser, the first CBA reactor and the first condenser until the second CBA reactor is completely regenerated, and at the same time, the tail gas is discharged to the tail gas incineration unit through the second interface of the second three-way valve;
the valve controller is used for switching the first three-way valve, so that a second interface of the first three-way valve is communicated with a third interface, and the states of other valves are unchanged, at the moment, the process gas from the Claus reactor is cooled through the Claus condenser, and the cooled process gas sequentially passes through the second CBA reactor, the second condenser, the third CBA reactor, the third condenser, the first CBA reactor and the first condenser, and meanwhile, the second interface of the second three-way valve is used for discharging tail gas to a tail gas incineration unit;
Through the valve controller, switch the fourth three-way valve, make the first interface and the second interface intercommunication of fourth three-way valve, simultaneously, open first two-way valve, the remaining valve state is unchangeable, and at this moment, the process gas from claus reactor cools off through claus condenser, and the process gas after the cooling off carries out in two ways:
part of the cooled process gas passes through the first CBA reactor and the first condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a second three-way valve; the other part of the cooled process gas sequentially passes through the second CBA reactor, the second condenser, the third CBA reactor and the third condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a fourth three-way valve;
through the valve controller, switch the second three-way valve, make the first interface and the third interface intercommunication of second three-way valve, simultaneously close the second two-way valve, other valve states are unchangeable, and at this moment, the process gas from claus reactor is cooled by claus condenser, and the process gas after the cooling is in proper order through first CBA reactor, first condenser, second CBA reactor, second condenser, third CBA reactor, third condenser is discharged tail gas by the second interface of fourth three-way valve to tail gas incineration unit simultaneously.
In some possible implementations, treating the tail gas with the tail gas incineration unit includes:
capturing the tail gas by using a tail gas catcher;
and introducing the trapped tail gas into a tail gas burning furnace for burning treatment.
The technical scheme provided by the embodiment of the invention has the beneficial effects that at least:
the low-temperature sulfur recovery system and the low-temperature sulfur recovery method provided by the embodiment of the invention enable the valve component to be configured to enable the regenerated CBA reactor to be positioned between the two adsorbed CBA reactors by switching the valve, and enable a large amount of hydrogen sulfide and sulfur dioxide gas contained in the regenerated CBA reactor and the catalyst pore not to directly enter the tail gas incineration unit any more but to pass through the back of the regenerated CBA reactorThe adsorbed CBA reactor at the end is subjected to a claus reaction and then enters a tail gas incineration unit. So arranged, H in the tail gas can be avoided 2 S and SO 2 Is beneficial to providing the recovery rate of sulfur at the same time.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for the description of the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a low-temperature sulfur recovery system according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram of a secondary reaction unit according to an embodiment of the present invention.
In fig. 2, AB marked in each three-way valve is used as a first interface, a marked a is used as a second interface, and B marked B is used as a third interface.
Other reference numerals denote:
an 11-claus reactor, a 12-claus condenser,
21-a first CBA reactor, 22-a second CBA reactor, 23-a third CBA reactor,
31-first condenser, 32-second condenser, 33-third condenser,
41-first three-way valve, 42-second three-way valve, 43-third three-way valve, 44-fourth three-way valve,
51-first two-way valve, 52-second two-way valve, 53-third two-way valve,
61-an acid gas separator, 62-an acid gas preheater, 63-a main fan, 64-an air preheater,
65-a main combustion furnace, 66-a waste heat boiler, 67-a front condenser, 68-a reheater and 69-an acid water pressure feeding tank,
71-tail gas catcher, 72-tail gas burning furnace,
8-liquid flow cell.
Detailed Description
In order to make the technical scheme and advantages of the present invention more apparent, embodiments of the present invention will be described in further detail with reference to the accompanying drawings.
The term "low temperature" used in the recovery of low-temperature sulfur in the embodiments of the present invention refers to a temperature lower than the dew point temperature of sulfur.
In one aspect, an embodiment of the present invention provides a low-temperature sulfur recovery system, including: the device comprises an acid gas preheating treatment unit, a main reaction unit, a secondary reaction unit and a tail gas incineration unit which are connected in sequence. Wherein the secondary reaction unit comprises: three CBA reactors and valve assemblies; the three CBA reactors are switched between a regeneration state and an adsorption state; the valve assembly is configured to position the regenerated CBA reactor between two adsorbed CBA reactors by switching the valve.
According to the low-temperature sulfur recovery system provided by the embodiment of the invention, the valve component is configured to enable the regenerated CBA reactor to be positioned between the two adsorbed CBA reactors through the switching valve, so that a large amount of hydrogen sulfide and sulfur dioxide gas contained in the regenerated CBA reactor and the catalyst pores do not directly enter the tail gas incineration unit any more, but enter the tail gas incineration unit after undergoing the Claus reaction through the adsorbed CBA reactor at the rear end of the regenerated CBA reactor. So arranged, H in the tail gas can be avoided 2 S and SO 2 Is beneficial to providing the recovery rate of sulfur at the same time.
In some possible implementations, as shown in fig. 1, the main reaction unit includes: a claus reactor 11, a claus condenser 12.
As shown in fig. 2, the secondary reaction unit includes: the first CBA reactor 21, the second CBA reactor 22, the third CBA reactor 23, the first condenser 31, the second condenser 32, the third condenser 33, the first three-way valve 41, the second three-way valve 42, the third three-way valve 43, the fourth three-way valve 44, the first two-way valve 51, the second two-way valve 52, the third two-way valve 53, and the valve controller (not shown in the figure).
The outlet of the claus reactor 11, the first port AB of the first three-way valve 41 are connected in sequence;
the outlet of the claus reactor 11, the claus condenser 12, the second port a of the first three-way valve 41 are connected in sequence;
the third port B of the first three-way valve 41, the first two-way valve 51, the first CBA reactor 21, the first condenser 31, and the first port AB of the second three-way valve 42 are sequentially connected;
the second interface A of the second three-way valve 42 is connected with the tail gas incineration unit, and the third interface B of the second three-way valve 42, the second CBA reactor 22, the second condenser 32 and the first interface AB of the third three-way valve 43 are sequentially connected;
The second port A of the third three-way valve 43 is connected with the tail gas incineration unit, and the third port B of the third three-way valve 43, the third CBA reactor 23, the third condenser 33 and the first port AB of the fourth three-way valve 44 are sequentially connected;
the second interface A of the fourth three-way valve 44 is connected with the tail gas incineration unit, and the third interface B of the fourth three-way valve 44 and the inlet of the first CBA reactor 21 are connected;
the second two-way valve 52 is located on the connecting line between the third port B of the first three-way valve 41 and the inlet of the second CBA reactor 22;
the third two-way valve 53 is located on the connection line between the third port B of the first three-way valve 41 and the inlet of the third CBA reactor 23;
a valve controller (not shown in the drawings) is configured to control the opening and closing operations of the first three-way valve 41, the second three-way valve 42, the third three-way valve 43, the fourth three-way valve 44, the first two-way valve 51, the second two-way valve 52, and the third two-way valve 53 so that the regenerated CBA reactor is located between the two CBA reactors of the two adsorbers.
In the embodiment of the invention, the first interface AB and the second interface A of each three-way valve are communicated in an angle, and the first interface AB and the third interface B are communicated. Moreover, the system provided by the embodiment of the invention further comprises: a liquid flow tank 8 for supplying circulating cold water to each condenser.
The embodiment of the invention exemplifies the situation of using three CBA reactors, wherein two CBA reactors are always in an adsorption reaction state, and sulfur obtained by reaction is adsorbedAbove the catalyst, the two CBA reactors operate at the dew point of the process gas sulfur, which is beneficial to the chemical reaction to proceed towards the direction of generating sulfur and improves the sulfur conversion. Because the temperature in the low-temperature adsorption-state converter is low and is close to the dew point of sulfur, solid sulfur is continuously attached to the surface of the catalyst, the activity of the catalyst is gradually lost, the temperature of the catalyst is required to be increased, the sulfur attached to the surface of the catalyst is removed, and the catalyst is regenerated. The other CBA reactor is subjected to high temperature regeneration and cooled after the regeneration to be used as a low temperature reactor. The embodiment of the invention has the improvement that each valve is switched by the valve controller so as to ensure that the CBA reactor cooled after regeneration is always positioned between two CBA reactors in an adsorption state, thereby ensuring H in tail gas on the premise of not influencing the recovery rate of sulfur 2 S and SO 2 The amount of (2) is always at a particularly low level.
In some possible implementations, as shown in fig. 1, an acid gas preheating unit provided in an embodiment of the present invention includes: the acid gas separator 61, the acid gas preheater 62, the main fan 63, the air preheater 64, the main combustion furnace 65, the waste heat boiler 66, the front condenser 67 and the reheater 68;
The acid gas separator 61, the acid gas preheater 62, the main combustion furnace 65, the waste heat boiler 66, the front condenser 67 and the reheater 68 are sequentially connected through pipelines; the main fan 63, the air preheater 64, and the main burner 65 are connected in sequence by pipelines.
In application, the acid gas to be treated, such as the acid gas from the desulfurization and decarbonization unit, is preheated by the acid gas preheater 62 after free water is separated by the acid gas separator 61, and the preheated acid gas enters the main combustion furnace 65. The air from the main fan 63 enters the main combustion furnace 65 after being preheated by the air preheater 64, and reacts with the acid gas entering the main combustion furnace 65 to lead H in the acid gas 2 S and SO 2 The ratio of (2) to (1) is maintained.
The high temperature process gas from the main burner 65 is cooled by heat exchange with a waste heat boiler 66, then cooled by a pre-condenser 67 and then heated by a reheater 68 to the appropriate claus reaction temperature.
As shown in fig. 1, the acid gas preheating treatment unit further includes: the acid water pressure feed tank 69 is connected to the acid gas separator 61, and the acid water pressure feed tank 69 is configured to receive the free water.
In some possible implementations, as shown in fig. 1, the tail gas incineration unit provided in the embodiment of the present invention includes: an exhaust gas catcher 71 and an exhaust gas burning furnace 72 are connected in sequence.
When the device is used, the tail gas is trapped by the tail gas trap 71, and the trapped tail gas is introduced into the tail gas burning furnace 72 for burning treatment.
On the other hand, the embodiment of the invention also provides a low-temperature sulfur recovery method, which adopts any one of the low-temperature sulfur recovery systems related to the embodiment of the invention.
In some possible implementation manners, the low-temperature sulfur recovery method provided by the embodiment of the invention includes the following steps:
step 1: and carrying out heat treatment on the acid gas to be treated by using an acid gas preheating treatment unit to obtain the acid gas to be treated with a set temperature.
Step 2: the acid gas to be treated with a set temperature is subjected to a claus reaction in a main reaction unit to obtain a process gas.
Step 3: the process gas is subjected to a claus reaction in a secondary reaction unit to obtain tail gas, wherein the gas discharged from the regenerated CBA reactor enters the next stage CBA reactor of adsorption.
Step 4: treating the tail gas by using a tail gas incineration unit to obtain exhaust gas, comprising: trapping the exhaust gas with an exhaust gas trap 71; the trapped tail gas is passed into a tail gas burning furnace 72 for combustion treatment.
The steps involved above are described below:
For step 1, heat treating the acid gas to be treated by using an acid gas preheating treatment unit to obtain the acid gas to be treated with a set temperature, the method may include the following steps:
in the acid gas preheating treatment unit, an acid gas separator 61, an acid gas preheater 62, a main combustion furnace 65, a waste heat boiler 66, a front condenser 67 and a reheater 68 are sequentially connected through pipelines; the main fan 63, the air preheater 64, and the main burner 65 are connected in sequence by pipelines.
For example, the acid gas to be treated from the desulfurization and decarbonization unit is separated from free water by the acid gas separator 61 and then enters the acid gas preheater 62 to be preheated to 218 ℃, and the preheated acid gas enters the main combustion furnace 65. The air from the main blower 63 is preheated to 218 ℃ by the air preheater 64 and then fed into the main burner 65 to supply oxygen and react with the sour gas fed into the main burner 65 to react H therein 2 S and SO 2 Is maintained at a ratio of 2:1.
The high-temperature acid gas generated by the main combustion furnace 65 is cooled to about 487 ℃ through heat exchange of the waste heat boiler 66 (improving the heat utilization rate), then part of the acid gas enters the front condenser 67 to be cooled to about 168 ℃, then the acid gas is heated to 218 ℃ by the reheater 68, and then the acid gas is mixed with the outlet gas of the waste heat boiler 66 to 280 ℃ and enters the Claus reactor 11.
For step 2, the acid gas to be treated with a set temperature is subjected to a claus reaction in a main reaction unit to obtain a process gas.
For example, al in the Claus reactor 11 of the main reaction unit of the acid gas to be treated at 280 DEG C 2 O 3 The conventional claus reaction takes place on the catalyst and the temperature is raised to 343 ℃.
For step 3, the process gas is subjected to claus reaction in turn in a secondary reaction unit to obtain tail gas, wherein the gas discharged from the regenerated CBA reactor enters the final CBA reactor of adsorption.
For example, the secondary reaction unit comprises: the first CBA reactor 21, the second CBA reactor 22, the third CBA reactor 23, the first condenser 31, the second condenser 32, the third condenser 33, the first three-way valve 41, the second three-way valve 42, the third three-way valve 43, the fourth three-way valve 44, the first two-way valve 51, the second two-way valve 52, the third two-way valve 53, and the valve controller.
The outlet of the claus reactor 11, the first port AB of the first three-way valve 41 are connected in sequence; the outlet of the claus reactor 11, the claus condenser 12, and the second port a of the first three-way valve 41 are connected in sequence.
The third port B of the first three-way valve 41, the first two-way valve 51, the first CBA reactor 21, the first condenser 31, and the first port AB of the second three-way valve 42 are sequentially connected; the second port a of the second three-way valve 42 is connected to the tail gas incineration unit, and the third port B of the second three-way valve 42, the second CBA reactor 22, the second condenser 32, and the first port AB of the third three-way valve 43 are sequentially connected.
The second port A of the third three-way valve 43 is connected with the tail gas incineration unit, and the third port B of the third three-way valve 43, the third CBA reactor 23, the third condenser 33 and the first port AB of the fourth three-way valve 44 are sequentially connected; the second port a of the fourth three-way valve 44 is connected to the tail gas incineration unit, and the third port B of the fourth three-way valve 44 is connected to the inlet of the first CBA reactor 21.
The second two-way valve 52 is located on the connecting line between the third port B of the first three-way valve 41 and the inlet of the second CBA reactor 22; the third two-way valve 53 is located on the connection line between the third port B of the first three-way valve 41 and the inlet of the third CBA reactor 23.
A valve controller (not shown in the drawings) is configured to control the opening and closing operations of the first three-way valve 41, the second three-way valve 42, the third three-way valve 43, the fourth three-way valve 44, the first two-way valve 51, the second two-way valve 52, and the third two-way valve 53 so that the regenerated CBA reactor is located between the two CBA reactors of the two adsorbers.
Based on the secondary reaction unit, the embodiment of the invention respectively explains the flow related to the low-temperature sulfur recovery method:
(1) The first CBA reactor 21 is regenerated and cooled
For this case, the low-temperature sulfur recovery method provided by the embodiment of the invention comprises the following steps:
Step 1, the first port AB of the first three-way valve 41 is communicated with the third port B through the valve controller, the first port AB of the second three-way valve 42 and the third three-way valve 43 are communicated with the third port B, the first port AB of the fourth three-way valve 44 is communicated with the second port a, the first two-way valve 51 is opened, the second two-way valve 52 and the third two-way valve 53 are closed, at this time, the process gas from the claus reactor 11 sequentially passes through the first CBA reactor 21, the first condenser 31, the second CBA reactor 22, the second condenser 32, the third CBA reactor 23 and the third condenser 33 until the first CBA reactor 21 is completely regenerated, and at the same time, the tail gas is discharged to the tail gas incineration unit through the second port a of the fourth three-way valve 44.
In this step 1, for example, the process gas from the claus reactor 11 is no longer passed through the claus condenser 12 and the hot process gas is preheated from the straight-through line directly into the first CBA reactor 21 until the temperature at the top of the catalyst bed of the first CBA reactor 21 will reach around 344 ℃, and the temperature at the bottom of the catalyst bed will be around 291 ℃ (for about 3.8 hours). Once the temperature of the first CBA reactor 21 reaches 291 ℃, sulfur will desorb from the catalyst (for about 3 hours) until the temperature of the entire catalyst bed will reach 344 ℃ and little sulfur in the catalyst will be present. Further, the hot process gas was heated on the catalyst bed for a further 30 minutes to complete the complete regeneration of the first CBA reactor, ensuring that all sulfur was fully desorbed from the catalyst bed.
Step 2, the first three-way valve 41 is switched through the valve controller, so that the second interface A and the third interface B of the first three-way valve 41 are communicated, and the states of the other valves are unchanged, at this time, the process gas from the claus reactor 11 is cooled through the claus condenser 12, and the cooled process gas sequentially passes through the first CBA reactor 21, the first condenser 31, the second CBA reactor 22, the second condenser 32, the third CBA reactor 23 and the third condenser 33, and meanwhile, the tail gas is discharged to the tail gas incineration unit through the second interface A of the fourth three-way valve 44.
For example, the 344 ℃ process gas from the claus reactor 11 is cooled to around 127 ℃ via the claus condenser 12, and the cooled process gas is passed through the first CBA reactor 21, so that the top of the catalyst bed will be cooled from 344 ℃ to around 127 ℃, and the bottom of the catalyst bed is cooled to around 244 ℃ (for about 3 hours) to achieve pre-cooling of the regenerated first CBA reactor 21.
Step 3, switching the third three-way valve 43 through the valve controller to enable the first port AB of the third three-way valve 43 to be communicated with the second port a, simultaneously opening the third two-way valve 53, and keeping the other valve states unchanged, wherein the process gas from the claus reactor 11 is cooled through the claus condenser 12, and the cooled process gas is divided into two paths:
Part of the cooled process gas passes through the third CBA reactor 23 and the third condenser 33, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface A of a fourth three-way valve 44; the other part of cooled process gas sequentially passes through the first CBA reactor 21, the first condenser 31, the second CBA reactor 22 and the second condenser 32, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface A of a third three-way valve 43;
step 4, switching the fourth three-way valve 44 through the valve controller, so that the first port AB of the fourth three-way valve 44 is communicated with the third port B, and simultaneously, the first two-way valve 51 is closed, and the other valve states are unchanged, at this time, the process gas from the claus reactor 11 is cooled by the claus condenser 12, and the cooled process gas sequentially passes through the third CBA reactor 23, the third condenser 33, the first CBA reactor 21, the first condenser 31, the second CBA reactor 22 and the second condenser 32, and meanwhile, the tail gas is discharged to the tail gas incineration unit through the second port a of the third three-way valve 43.
At this time, the first CBA reactor 21 was adsorbed and finally cooled for 3 hours, and the space of the first CBA reactor 21 and the catalyst pores contained a higher concentration of the process gas H 2 S and SO 2 The reaction can be carried out again in the second reactor of the final stage, instead of directly into the tail gas incineration unit.
The sequence of steps 3 and 4 must be followed exactly to ensure that there is always a path to the tail gas burning furnace 72 of the tail gas incineration unit.
By analogy, the second CBA reactor 22 and the third CBA reactor 23 regeneration and adsorption procedure is as shown above. The regenerated CBA reactor is always in the middle position, not the last stage position. The following are respectively illustrated:
(2) The third CBA reactor 23 is regenerated and cooled
For this case, the low-temperature sulfur recovery method provided by the embodiment of the invention further comprises the following steps:
step 5, the first port AB of the first three-way valve 41 is communicated with the third port B through the valve controller, the first port AB of the second three-way valve 42 and the fourth three-way valve 44 are communicated with the third port B, the first port AB of the third three-way valve 43 is communicated with the second port a, the third two-way valve 53 is opened, the second two-way valve 52 and the first two-way valve 51 are closed, at this time, the process gas from the claus reactor 11 sequentially passes through the third CBA reactor 23, the third condenser 33, the first CBA reactor 21, the first condenser 31, the second CBA reactor 22 and the second condenser 32 until the third CBA reactor 23 is completely regenerated, and at the same time, the tail gas is discharged to the tail gas incineration unit through the second port a of the third three-way valve 43.
Specific operations are described above with reference to the example of step 1.
Step 6, the first three-way valve 41 is switched through the valve controller, so that the second port A of the first three-way valve 41 is communicated with the third port B, and the rest valve states are unchanged, at this time, the process gas from the Claus reactor 11 is cooled through the Claus condenser 12, and the cooled process gas sequentially passes through the third CBA reactor 23, the third condenser 33, the first CBA reactor 21, the first condenser 31, the second CBA reactor 22 and the second condenser 32, and meanwhile, the tail gas is discharged to the tail gas incineration unit through the second port A of the third three-way valve 43.
Step 7, through the valve controller, the second three-way valve 42 is switched, so that the first port AB of the second three-way valve 42 is communicated with the second port a, meanwhile, the second two-way valve 52 is opened, and the other valve states are unchanged, at this time, the process gas from the claus reactor 11 is cooled by the claus condenser 12, and the cooled process gas is divided into two paths:
a part of cooled process gas passes through the second CBA reactor 22 and the second condenser 32, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface A of the third three-way valve 43; the other part of the cooled process gas sequentially passes through the third CBA reactor 23, the third condenser 33, the first CBA reactor 21 and the first condenser 31, and the tail gas is discharged to the tail gas incineration unit through the second interface A of the second three-way valve 42.
Specific operations are described above with reference to the example of step 2.
Step 8, switching the third three-way valve 43 through the valve controller to enable the first port AB and the third port B of the third three-way valve 43 to be communicated, closing the third two-way valve 53 at the same time, and keeping the other valve states unchanged, wherein at the moment, the process gas from the Claus reactor 11 is cooled through the Claus condenser 12, and the cooled process gas sequentially passes through the second CBA reactor 22, the second condenser 32, the third CBA reactor 23, the third condenser 33, the first CBA reactor 21, the first condenser 31 and the second port A of the second three-way valve 42 to discharge the tail gas to the tail gas incineration unit.
(3) The fourth CBA reactor is regenerated and cooled
For this case, the low-temperature sulfur recovery method provided by the embodiment of the invention further comprises the following steps:
step 9, the first port AB of the first three-way valve 41 is communicated with the third port B through the valve controller, the first port AB of the third three-way valve 43 and the fourth three-way valve 44 are communicated with the third port B, the first port AB of the first three-way valve 41 is communicated with the second port a, the second two-way valve 52 is opened, the third two-way valve 53 and the first two-way valve 51 are closed, at this time, the process gas from the claus reactor 11 sequentially passes through the second CBA reactor 22, the second condenser 32, the third CBA reactor 23, the third condenser 33, the first CBA reactor 21 and the first condenser 31 until the second CBA reactor 22 is completely regenerated, and at the same time, the tail gas is discharged to the tail gas incineration unit through the second port a of the second three-way valve 42.
Specific operations are described above with reference to the example of step 1.
Step 10, the first three-way valve 41 is switched through the valve controller, so that the second port A and the third port B of the first three-way valve 41 are communicated, and the states of the other valves are unchanged, at this time, the process gas from the Claus reactor 11 is cooled through the Claus condenser 12, and the cooled process gas sequentially passes through the second CBA reactor 22, the second condenser 32, the third CBA reactor 23, the third condenser 33, the first CBA reactor 21 and the first condenser 31, and meanwhile, the tail gas is discharged to the tail gas incineration unit through the second port A of the second three-way valve 42.
Specific operations are described above with reference to the example of step 2.
Step 11, through the valve controller, the fourth three-way valve 44 is switched, so that the first port AB of the fourth three-way valve 44 is communicated with the second port a, meanwhile, the first two-way valve 51 is opened, and the other valve states are unchanged, at this time, the process gas from the claus reactor 11 is cooled by the claus condenser 12, and the cooled process gas is divided into two paths:
a part of cooled process gas passes through the first CBA reactor 21 and the first condenser 31, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface A of the second three-way valve 42; the other part of the cooled process gas sequentially passes through the second CBA reactor 22, the second condenser 32, the third CBA reactor 23 and the third condenser 33, and the tail gas is discharged to the tail gas incineration unit through the second interface A of the fourth three-way valve 44.
Step 12, through the valve controller, the second three-way valve 42 is switched, so that the first port AB of the second three-way valve 42 is communicated with the third port B, meanwhile, the second two-way valve 52 is closed, and the other valve states are unchanged, at this time, the process gas from the claus reactor 11 is cooled by the claus condenser 12, and the cooled process gas sequentially passes through the first CBA reactor 21, the first condenser 31, the second CBA reactor 22, the second condenser 32, the third CBA reactor 23 and the third condenser 33, and meanwhile, the tail gas is discharged to the tail gas incineration unit through the second port a of the fourth three-way valve 44.
In the low-temperature sulfur recovery method provided by the embodiment of the invention, the switching sequence of each three-way valve and two-way valve in the low-temperature sulfur recovery system is changed, so that the process gas H with higher concentration in the space of the pre-cooled CBA reactor after regeneration and in the catalyst pore is formed 2 S and SO 2 The adsorption-state CBA reactor at the rear end of the regenerated pre-cooled CBA reactor absorbs and reacts instead of directly entering the tail gas incineration unit, SO that SO in the tail gas can be effectively reduced 2 Is arranged in the air.
The process is realized by changing the switching sequence of each three-way valve and each two-way valve in the low-temperature sulfur recovery system, SO that the method provided by the embodiment of the invention reduces the SO of the tail gas with minimum investment and maximum efficiency 2 Emission amount is reducedLess influence on environment and better environmental benefit.
In embodiments of the present invention, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. The term "plurality" refers to two or more, unless explicitly defined otherwise.
The foregoing description is only for the convenience of those skilled in the art to understand the technical solution of the present invention, and is not intended to limit the present invention. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (7)

1. A low temperature sulfur recovery system, the low temperature sulfur recovery system comprising: the device comprises an acid gas preheating treatment unit, a main reaction unit, a secondary reaction unit and a tail gas incineration unit which are connected in sequence;
wherein the secondary reaction unit comprises: three CBA reactors and valve assemblies;
the three CBA reactors are switched between a regeneration state and an adsorption state;
the valve assembly is configured to position the regenerated CBA reactor between two adsorbed CBA reactors by switching the valve;
the main reaction unit includes: a claus reactor, a claus condenser;
The secondary reaction unit includes: the system comprises a first CBA reactor, a second CBA reactor, a third CBA reactor, a first condenser, a second condenser, a third condenser, a first three-way valve, a second three-way valve, a third three-way valve, a fourth three-way valve, a first two-way valve, a second two-way valve, a third two-way valve and a valve controller;
the outlet of the Claus reactor and the first interface of the first three-way valve are sequentially connected;
the outlet of the claus reactor, the claus condenser and the second interface of the first three-way valve are sequentially connected;
the third interface of the first three-way valve, the first two-way valve, the first CBA reactor, the first condenser and the first interface of the second three-way valve are sequentially connected;
the second interface of the second three-way valve is connected with the tail gas incineration unit, and the third interface of the second three-way valve, the second CBA reactor, the second condenser and the first interface of the third three-way valve are sequentially connected;
the second interface of the third three-way valve is connected with the tail gas incineration unit, and the third interface of the third three-way valve, the third CBA reactor, the third condenser and the first interface of the fourth three-way valve are sequentially connected;
The second interface of the fourth three-way valve is connected with the tail gas incineration unit, and the third interface of the fourth three-way valve and the inlet of the first CBA reactor are connected;
the second two-way valve is positioned on a connecting pipeline between a third interface of the first three-way valve and an inlet of the second CBA reactor;
the third two-way valve is positioned on a connecting pipeline between a third interface of the first three-way valve and an inlet of the third CBA reactor;
the valve controller is configured to control opening and closing operations of the first three-way valve, the second three-way valve, the third three-way valve, the fourth three-way valve, the first two-way valve, the second two-way valve and the third two-way valve so that the regenerated CBA reactor is positioned between the two CBA reactors;
the acid gas preheating treatment unit comprises: the system comprises an acid-gas separator, an acid-gas preheater, a main fan, an air preheater, a main combustion furnace, a waste heat boiler, a front condenser and a reheater;
the acid gas separator, the acid gas preheater, the main combustion furnace, the waste heat boiler, the front condenser and the reheater are sequentially connected through pipelines;
The main fan, the air preheater and the main combustion furnace are sequentially connected through pipelines;
the acid gas preheating treatment unit is used for heating the acid gas to the Claus reaction temperature,h in sour gas 2 S and SO 2 Is maintained at a ratio of 2:1.
2. The low temperature sulfur recovery system of claim 1, wherein the tail gas incineration unit comprises: the tail gas catcher and the tail gas burning furnace are connected in sequence.
3. A low-temperature sulfur recovery method, characterized in that the low-temperature sulfur recovery method adopts the low-temperature sulfur recovery system according to any one of claims 1-2;
the low-temperature sulfur recovery method comprises the following steps:
carrying out heat treatment on the acid gas to be treated by using an acid gas preheating treatment unit to obtain the acid gas to be treated with a set temperature;
carrying out a claus reaction on the acid gas to be treated with the set temperature in the main reaction unit to obtain a process gas;
carrying out claus reaction on the process gas in the secondary reaction unit to obtain tail gas, wherein the gas discharged from the regenerated CBA reactor enters an adsorbed final-stage CBA reactor;
and treating the tail gas by using the tail gas incineration unit to obtain exhaust gas.
4. The method for recovering low-temperature sulfur according to claim 3, wherein the method for recovering low-temperature sulfur comprises: the first interface of the first three-way valve is communicated with the third interface, the first interface of the second three-way valve and the third three-way valve are communicated with the third interface, the first interface of the fourth three-way valve is communicated with the second interface, the first two-way valve is opened, the second two-way valve and the third two-way valve are closed, at the moment, the process gas from the Claus reactor sequentially passes through the first CBA reactor, the first condenser, the second CBA reactor, the second condenser, the third CBA reactor and the third condenser until the first CBA reactor is completely regenerated, and at the same time, the second interface of the fourth three-way valve discharges tail gas to a tail gas incineration unit;
the valve controller is used for switching the first three-way valve, so that a second interface of the first three-way valve is communicated with a third interface, and the states of other valves are unchanged, at the moment, the process gas from the Claus reactor is cooled through the Claus condenser, and the cooled process gas sequentially passes through the first CBA reactor, the first condenser, the second CBA reactor, the second condenser, the third CBA reactor and the third condenser, and meanwhile, the second interface of the fourth three-way valve is used for discharging tail gas to a tail gas incineration unit;
Through the valve controller, the third three-way valve is switched, so that the first interface and the second interface of the third three-way valve are communicated, meanwhile, the third two-way valve is opened, the states of other valves are unchanged, at the moment, the process gas from the Claus reactor is cooled by the Claus condenser, and the cooled process gas is divided into two paths:
part of the cooled process gas passes through the third CBA reactor and the third condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a fourth three-way valve; the other part of the cooled process gas sequentially passes through the first CBA reactor, the first condenser, the second CBA reactor and the second condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a third three-way valve;
through the valve controller, switch the fourth three-way valve, make the first interface and the third interface intercommunication of fourth three-way valve, simultaneously close first two-way valve, the remaining valve state is unchangeable, and at this moment, the process gas from claus reactor is cooled by claus condenser, and the process gas after the cooling is in proper order through third CBA reactor third condenser first CBA reactor first condenser second CBA reactor second condenser simultaneously is discharged tail gas by the second interface of third three-way valve to tail gas incineration unit.
5. The method for recovering sulfur at low temperature according to claim 4, further comprising:
the first interface of the first three-way valve is communicated with the third interface, the first interfaces of the second three-way valve and the fourth three-way valve are communicated with the third interface, the first interface of the third three-way valve is communicated with the second interface, the third two-way valve is opened, the second two-way valve and the first two-way valve are closed, and at the moment, the process gas from the Claus reactor sequentially passes through the third CBA reactor, the third condenser, the first CBA reactor, the first condenser, the second CBA reactor and the second condenser until the third CBA reactor is completely regenerated, and at the same time, the tail gas is discharged to the tail gas incineration unit through the second interface of the third three-way valve;
the valve controller is used for switching the first three-way valve, so that a second interface of the first three-way valve is communicated with a third interface, and the states of other valves are unchanged, at the moment, the process gas from the Claus reactor is cooled through the Claus condenser, and the cooled process gas sequentially passes through the third CBA reactor, the third condenser, the first CBA reactor, the first condenser, the second CBA reactor and the second condenser, and meanwhile, the second interface of the third three-way valve is used for discharging tail gas to a tail gas incineration unit;
Through the valve controller, switch the second three-way valve, make the first interface and the second interface intercommunication of second three-way valve, simultaneously, open the second two-way valve, the remaining valve state is unchangeable, and at this moment, the process gas from claus reactor cools off through claus condenser, and the process gas after the cooling off carries out in two ways:
part of the cooled process gas passes through the second CBA reactor and the second condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a third three-way valve; the other part of the cooled process gas sequentially passes through the third CBA reactor, the third condenser, the first CBA reactor and the first condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a second three-way valve;
through the valve controller, switch the third three-way valve, make the first interface and the third interface intercommunication of third three-way valve, simultaneously close the third two-way valve, the remaining valve state is unchangeable, and at this moment, the process gas from claus reactor is cooled by claus condenser, and the process gas after the cooling is in proper order through the second CBA reactor second condenser third CBA reactor third condenser first CBA reactor first condenser, exhaust gas is discharged to tail gas incineration unit by the second interface of second three-way valve simultaneously.
6. The method for recovering sulfur at low temperature according to claim 5, further comprising:
the first interface of the first three-way valve is communicated with the third interface through the valve controller, the first interfaces of the third three-way valve and the fourth three-way valve are communicated with the third interface, the first interface of the first three-way valve is communicated with the second interface, the second two-way valve is opened, the third two-way valve and the first two-way valve are closed, and at the moment, the process gas from the Claus reactor sequentially passes through the second CBA reactor, the second condenser, the third CBA reactor, the third condenser, the first CBA reactor and the first condenser until the second CBA reactor is completely regenerated, and at the same time, the tail gas is discharged to the tail gas incineration unit through the second interface of the second three-way valve;
the valve controller is used for switching the first three-way valve, so that a second interface of the first three-way valve is communicated with a third interface, and the states of other valves are unchanged, at the moment, the process gas from the Claus reactor is cooled through the Claus condenser, and the cooled process gas sequentially passes through the second CBA reactor, the second condenser, the third CBA reactor, the third condenser, the first CBA reactor and the first condenser, and meanwhile, the second interface of the second three-way valve is used for discharging tail gas to a tail gas incineration unit;
Through the valve controller, switch the fourth three-way valve, make the first interface and the second interface intercommunication of fourth three-way valve, simultaneously, open first two-way valve, the remaining valve state is unchangeable, and at this moment, the process gas from claus reactor cools off through claus condenser, and the process gas after the cooling off carries out in two ways:
part of the cooled process gas passes through the first CBA reactor and the first condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a second three-way valve; the other part of the cooled process gas sequentially passes through the second CBA reactor, the second condenser, the third CBA reactor and the third condenser, and meanwhile, the tail gas is discharged to a tail gas incineration unit through a second interface of a fourth three-way valve;
through the valve controller, switch the second three-way valve, make the first interface and the third interface intercommunication of second three-way valve, simultaneously close the second two-way valve, other valve states are unchangeable, and at this moment, the process gas from claus reactor is cooled by claus condenser, and the process gas after the cooling is in proper order through first CBA reactor, first condenser, second CBA reactor, second condenser, third CBA reactor, third condenser is discharged tail gas by the second interface of fourth three-way valve to tail gas incineration unit simultaneously.
7. The method for recovering sulfur at low temperature according to any one of claims 3 to 6, wherein treating the tail gas with the tail gas incineration unit comprises:
capturing the tail gas by using a tail gas catcher;
and introducing the trapped tail gas into a tail gas burning furnace for burning treatment.
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FR2142780B1 (en) * 1971-06-24 1973-06-29 Inst Francais Du Petrole
US4844881A (en) * 1986-02-24 1989-07-04 The Boc Group, Inc. Process for the production of sulfur from hydrogen sulfide using high concentration oxygen and recycle in combination with a scrubbing tower
CN100588608C (en) * 2007-04-30 2010-02-10 中国石油集团工程设计有限责任公司 The improvement low-temperature Claus sulfur recovery method
CN101289170B (en) * 2008-06-13 2010-08-25 西安思瑞迪精馏工程有限公司 Oxidation, reduction and sulfur recovery multipurpose device
CN102556977B (en) * 2010-12-30 2013-12-04 中国石油天然气股份有限公司 Inner cooling type direct oxidation recycling method and recycling device of sulfur
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