CN112337280B - Claus split-flow sulfur recovery system and process - Google Patents
Claus split-flow sulfur recovery system and process Download PDFInfo
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Abstract
The invention relates to the field of natural gas purification and coal chemical industry, and discloses a Claus shunting sulfur recovery system and a process, wherein the system comprises an acid gas shunting part, an acid gas/process gas thermal reaction mixing part, a process gas condensing/preheating part and a catalytic reaction part; an acid gas outlet of the acid gas separating part is communicated with an acid gas inlet of the acid gas separating part, an acid gas outlet of the acid gas separating part is communicated with an acid gas inlet of the acid gas/process gas thermal reaction mixing part, a thermal reaction process gas outlet of the acid gas/process gas thermal reaction mixing part is communicated with a thermal reaction process gas inlet of the process gas condensing/preheating part, a pre-catalysis process gas outlet of the process gas condensing/preheating part is communicated with a pre-catalysis process gas inlet of the catalytic reaction part, and a post-catalysis process gas inlet of the process gas condensing/preheating part is communicated with a post-catalysis process gas outlet of the catalytic reaction part. The invention has high sulfur production conversion rate, less carbon deposition and low energy consumption.
Description
Technical Field
The invention relates to the fields of natural gas purification and coal chemical industry, in particular to a Claus split-flow sulfur recovery system and a Claus split-flow sulfur recovery process.
Background
H removal from natural gas or raw coal in the fields of natural gas purification and coal chemical industry 2 The S must be sent to a sulphur recovery unit to convert most of the elemental sulphur to a sulphur product. H in acid gas generated in the above field 2 Concentration of SThe degree is generally lower, namely the lean acid gas, and the ammonia liquid, the hydrocarbon and the CO are simultaneously contained 2 And the treatment difficulty is far higher than that of acid gas in a refinery due to impurities.
If the sulfur recovery device adopts the currently commonly applied Claus direct current process, because the concentration of the acid gas is low, in order to ensure the lowest stable temperature of the reaction furnace, a large amount of fuel gas is generally injected into the reaction furnace for combustion, so that the combustion temperature of the reaction furnace is improved, and the energy consumption of the device is large; the conversion rate of the sulfur recovery device is low due to severe side reaction in the reaction furnace; an increase in the process gas quantity also leads to an increase in the plant investment.
The sulphur recovery unit may also employ a claus split process. According to the concentration of the acid gas, a part of the acid gas (generally accounting for more than 33 percent of the total gas amount) directly enters the reaction furnace for combustion, and most of H is generated 2 S to SO 2 Thereby increasing the combustion temperature of the reaction furnace. And cooling the combusted process gas by a waste heat boiler of the reaction furnace, mixing the cooled process gas with the other part of the acid gas, and allowing the mixture to enter a Claus reactor for subsequent catalytic reaction. The process can ensure the stable combustion of the reaction furnace and improve the operation stability of the sulfur recovery device, but because a part of acid gas directly enters a catalytic reaction stage without thermal reaction, the load of the catalytic reaction is increased, the catalytic dosage needs to be improved, and the sulfur recovery rate of the device is reduced; the acid gas often carries hydrocarbon impurities, which easily causes carbon deposition and inactivation of the catalyst, shortens the service life of the catalyst and influences the long-period operation of the sulfur recovery device.
Disclosure of Invention
In view of the foregoing, it is an object of the present invention to provide a Claus split sulfur recovery system and process for treating low H sulfur 2 Acid gas with S concentration, and recovering H therein 2 S, the system and the process have the advantages of both the direct-current process and the shunt process, and simultaneously overcome the defects of the two processes.
The first aspect of the invention provides a Claus split-flow sulfur recovery system, which comprises an acid gas split-flow part, an acid gas/process gas thermal reaction mixing part, a process gas condensing/preheating part and a catalytic reaction part;
the acid gas outlet of the acid gas separating part is communicated with the acid gas inlet of the acid gas separating part, the front diversion acid gas outlet and the rear diversion acid gas outlet of the acid gas separating part are respectively communicated with the front diversion acid gas inlet and the rear diversion acid gas inlet of the acid gas/process gas thermal reaction mixing part, the thermal reaction process gas outlet of the acid gas/process gas thermal reaction mixing part is communicated with the thermal reaction process gas inlet of the process gas condensing/preheating part, the pre-catalysis process gas outlet of the process gas condensing/preheating part is communicated with the pre-catalysis process gas inlet of the catalytic reaction part, and the post-catalysis process gas inlet of the process gas condensing/preheating part is communicated with the post-catalysis process gas outlet of the catalytic reaction part.
A second aspect of the invention provides a claus split sulphur recovery process comprising the steps of:
1) feeding the sulfur recovery acid gas into an acid gas liquid separation part, separating impurities carried in the sulfur recovery acid gas by an acid gas liquid separation facility, and pressurizing and delivering separated condensate out of the device by an acid gas condensate pump;
2) step 1), the purified acid gas enters an acid gas diversion part, and a diversion proportion calculation control device of the acid gas diversion part controls the acid gas diversion proportion according to the acid gas composition and the front region temperature and the rear region temperature of a reaction furnace of the acid gas/process gas thermal reaction mixing part, so that the acid gas is divided into front diversion acid gas and rear diversion acid gas;
3) the front shunting acid gas obtained in the step 2) is fully combusted with combustion air through a combustor of an acid gas/process gas thermal reaction mixing part, enters a reaction furnace and is mixed with a rear shunting acid gas in a mixing and strengthening facility;
4) cooling the process gas generated in the step 3) after the high-temperature thermal reaction by a condenser of a process gas condensing/preheating part to separate sulfur generated in the thermal reaction process, heating the process gas to the temperature of the catalytic reaction by a preheater, and then feeding the process gas into a catalytic reactor of a catalytic reaction part for reaction;
the catalytic reactor comprises two or more stages, the reaction product of the previous stage catalytic reactor is cooled by a condenser, the generated sulfur is separated out, the sulfur is preheated and enters the next stage catalytic reactor for reaction, and the process gas after the reaction of the last stage catalytic reactor enters the subsequent treatment stage through condensation.
The Claus shunting sulfur recovery system and the process of the invention can ensure the reaction conversion rate of the device, improve the adaptability to the concentration of acid gas and prolong the service life of the catalyst; the method meets the requirement of stable operation, simultaneously improves the conversion rate in the thermal reaction stage to the maximum extent, ensures the stable combustion of the reaction furnace, and successfully overcomes the problems of catalysis and carbon deposition caused by hydrocarbon impurities in the acid gas; when the invention is used for treating low-concentration acid gas, the conversion rate of the sulfur production part reaches more than 95 percent under the condition of ensuring the stable operation of the device.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without limiting the invention.
FIG. 1 is a schematic process flow diagram of a Claus split sulfur recovery system according to one embodiment of the present invention.
Description of the reference numerals
1 acid gas liquid separation part; 2 acid gas split part; 3 acid gas/process gas thermal reaction mixing part; 4 process gas condensing/preheating section; 5 a catalytic reaction part; 6 acid gas liquid separation facilities; 7 acid gas condensate pump; 8, a burner and a reaction furnace; 9 a condenser; 10, a preheater; 11 acid gas feed; 12 acid gas condensate; after 13, acid gas is shunted; acid gas is branched before 14 days; 15 thermally reacting the process gas; 16 primary pre-catalytic process gas; 17, carrying out primary catalysis on the process gas; 18 secondary pre-catalytic process gas; 19 secondary catalyzing the process gas; 20, tail gas; 21 liquid sulfur; 22 a coolant; 23 the coolant is returned.
Detailed Description
In order that the present invention may be more readily understood, the following detailed description of the invention is given with reference to the accompanying drawings and embodiments, which are given by way of illustration only and are not intended to limit the invention.
According to a first aspect of the invention, there is provided a claus split sulphur recovery system comprising an acid gas splitting section, an acid gas/process gas thermal reaction mixing section, a process gas condensing/preheating section and a catalytic reaction section;
the acid gas outlet of the acid gas separating part is communicated with the acid gas inlet of the acid gas separating part, the front diversion acid gas outlet and the rear diversion acid gas outlet of the acid gas separating part are respectively communicated with the front diversion acid gas inlet and the rear diversion acid gas inlet of the acid gas/process gas thermal reaction mixing part, the thermal reaction process gas outlet of the acid gas/process gas thermal reaction mixing part is communicated with the thermal reaction process gas inlet of the process gas condensing/preheating part, the pre-catalysis process gas outlet of the process gas condensing/preheating part is communicated with the pre-catalysis process gas inlet of the catalytic reaction part, and the post-catalysis process gas inlet of the process gas condensing/preheating part is communicated with the post-catalysis process gas outlet of the catalytic reaction part.
According to the invention, the acid gas liquid separation part comprises an acid gas liquid separation facility and an acid gas condensate pump, wherein an acid gas inlet of the acid gas liquid separation facility is communicated with a sulfur recovery acid gas feeding pipeline, an acid gas outlet of the acid gas liquid separation facility is communicated with an acid gas inlet of the acid gas liquid separation part, and a condensate outlet of the acid gas liquid separation facility is communicated with the acid gas condensate pipeline through the acid gas condensate pump. The sulfur recovery acid gas feed is separated from carried liquid drops through an acid gas liquid separation facility and enters an acid gas flow separation part, and separated condensate is sent out through an acid gas condensate pump.
In the invention, the acid gas liquid separation facility is provided with a separation internal part, and the specific composition of the separation internal part can be set according to the composition of the acid gas. When the acid gas impurity is mainly H 2 In the case of O, hydrocarbon and amine liquid, a wire mesh demister or a cyclone separator can be arranged to separate carried impuritiesQuality; the acid gas impurities contain a small amount of NH 3 And a spraying facility is required to be additionally arranged to wash the acid gas, and desalted water or production water is injected into the liquid separation facility, so that the influence of impurities on downstream equipment is reduced.
The acid gas condensate pump can be automatically started and stopped according to the liquid level height of the acid gas liquid separation facility. When the liquid separation facility is at a high liquid level, the acid gas condensate pump is started to send condensate to the acid gas condensate pipeline; and when the liquid separating facility is at a low liquid level, the acid gas condensate pump automatically stops. The acid gas condensate pump adopts a shield pump, and the driving form adopts electric driving.
In the invention, the acid gas diversion part comprises a diversion ratio calculation control device, the diversion ratio calculation control device comprises a control module, an acid gas composition on-line analyzer, a front region temperature meter and a rear region temperature meter, the signal input end of the acid gas composition on-line analyzer is positioned on an acid gas outlet pipeline of the acid gas liquid separation facility, the signal input end of the front region temperature meter is positioned at the front region of a reaction furnace of the acid gas/process gas thermal reaction mixing part, the signal input end of the rear region temperature meter is positioned at the outlet of the reaction furnace, and the signal output end of the acid gas composition on-line analyzer, the signal output end of the front region temperature meter and the signal output end of the rear region temperature meter are respectively communicated with the signal inlet of the control module.
The control module determines the acid gas shunting proportion according to the analysis data of the acid gas composition on-line analyzer, the temperature data of the front region temperature measuring meter, the temperature data of the rear region temperature measuring meter and the flow data of the acid gas, and outputs shunting control signals.
The front region temperature measuring meter and the rear region temperature measuring meter can adopt infrared optical thermometers, and the infrared radiation intensity of the reaction furnace is converted into the combustion/reaction temperature; a high temperature ceramic thermocouple thermometer may also be used, with the temperature sensing element located within the ceramic sleeve.
The acid gas diversion part can artificially increase the temperature set value to replace the value of the temperature measuring meter, and the set value is generally between 1000 ℃ and 1200 ℃ so as to improve the operation stability of the device.
According to the material flow direction, the acid gas/process gas thermal reaction mixing part comprises a combustor, a reaction furnace and a mixing strengthening facility which are sequentially communicated, wherein the combustor is provided with a combustion air inlet and a front diversion acid gas inlet, the combustion air inlet is communicated with a combustion air pipeline, the front diversion acid gas inlet is communicated with a front diversion acid gas outlet of the acid gas diversion part, the mixing strengthening facility is provided with a rear diversion acid gas inlet and a thermal reaction process gas outlet, the rear diversion acid gas inlet is communicated with a rear diversion acid gas outlet of the acid gas diversion part, and the thermal reaction process gas outlet is communicated with a thermal reaction process gas inlet of the process gas condensation/preheating part.
The front shunting acid gas from the acid gas shunting part is fully mixed with combustion air in a combustor, then is combusted in a combustion chamber of the combustor and then enters a reaction furnace, the temperature of a front zone of the reaction furnace is generally between 950-1300 ℃, the temperature of a rear zone is between 700-980 ℃ according to the composition of the acid gas, the process gas and the rear shunting acid gas after combustion reaction are subjected to forced mixing and heat recovery through a mixing and strengthening facility, and the process gas at the outlet of the hot reaction process gas of the mixing and strengthening facility enters a process gas condensation/preheating part.
In the invention, the process gas condensation/preheating part comprises a condenser and a preheater, the number of stages of the condenser and the preheater is matched with the number of stages of a catalytic reactor of the catalytic reaction part, the condenser is provided with a thermal reaction process gas inlet, a condensed process gas outlet and a catalyzed process gas inlet, the preheater is provided with a condensed process gas inlet and a pre-catalyzed process gas outlet, the thermal reaction process gas inlet is communicated with the thermal reaction process gas outlet of the acid gas/process gas thermal reaction mixing part, the condensed process gas outlet is communicated with the condensed process gas inlet, the pre-catalyzed process gas outlet is communicated with the pre-catalyzed process gas inlet, and the catalyzed process gas inlet is communicated with the post-catalyzed process gas outlet. In addition, a tail gas outlet of the process gas condensation/preheating part is communicated with a sulfur production tail gas pipeline, and a liquid sulfur outlet of the process gas condensation/preheating part is communicated with a liquid sulfur product pipeline.
The coolant of the condenser is low-pressure boiler water which generates low-pressure or low-pressure steam, or high-pressure boiler feed water. The heating medium of the preheater usually adopts high-pressure steam, the cooled high-pressure steam condensate water returns to the condensate water pipe network, and the preheater can also be heated by a heating furnace. The condenser can be designed integrally and share the same shell.
According to the invention, the catalytic reaction part comprises two or more stages of catalytic reactors, two or more catalysts are filled in the catalytic reactors, the bottoms of the catalysts are provided with supports, the upper layer is provided with inert ceramic balls, and the catalytic reactors are provided with a pre-catalytic process gas inlet and a post-catalytic process gas outlet.
In the catalytic reactor, the process gas undergoes a catalytic reaction, H 2 S and SO 2 Reaction for producing elemental sulfur, COS and CS 2 H production by hydrolysis of organic sulfur 2 S and CO 2 . For some catalytic reactions, H may also occur 2 S and O 2 Reaction to produce elemental sulfur. The catalytic reaction releases a large amount of heat, so that the temperature of the process gas at the outlet of the catalyzed process gas reaches between 220 ℃ and 330 ℃, and the process gas needs to be returned to the condensation/preheating part of the process gas for cooling.
The stage number of the catalytic reactor is set according to the requirement of the recovery rate, the higher the recovery rate requirement is, the more the stage number is, and the two stage catalytic reactor is generally adopted. The catalytic reactor can be designed integrally.
When the catalytic reaction part comprises two stages of catalytic reactors, a thermal reaction process gas inlet, a condensed process gas outlet, a first-stage catalyzed process gas inlet and a second-stage catalyzed process gas inlet are arranged on the condenser, a condensed process gas inlet, a first-stage catalyzed pre-process gas outlet and a second-stage catalyzed pre-process gas outlet are arranged on the preheater, the thermal reaction process gas inlet is communicated with the thermal reaction process gas outlet of the acid gas/process gas thermal reaction mixing part, the condensed process gas outlet is communicated with the condensed process gas inlet, the first-stage catalyzed pre-process gas outlet is communicated with the first-stage catalyzed pre-process gas inlet arranged on the first-stage catalytic reactor, the second-stage catalyzed pre-process gas outlet is communicated with the second-stage catalyzed pre-process gas inlet arranged on the second-stage catalytic reactor, the first-stage catalyzed post-process gas inlet is communicated with the first-stage catalyzed process gas outlet arranged on the first-stage catalytic reactor, and the secondary catalyzed process gas inlet is communicated with a secondary catalyzed process gas outlet arranged on the secondary catalytic reactor. In addition, the stage number of the condenser and the preheater is matched with the stage number of the catalytic reactor, so that the process gas reaches the temperature of the corresponding catalytic reactor before and after reaction.
According to a second aspect of the invention, there is provided a claus split sulphur recovery process comprising the steps of:
1) feeding the sulfur recovery acid gas into an acid gas liquid separation part, separating impurities carried in the sulfur recovery acid gas by an acid gas liquid separation facility, and pressurizing and delivering separated condensate out of the device by an acid gas condensate pump;
2) step 1), the purified acid gas enters an acid gas flow dividing part, and a flow dividing proportion calculation control device of the acid gas flow dividing part controls the acid gas flow dividing proportion according to the acid gas composition and the front zone temperature and the rear zone temperature of a reaction furnace of the acid gas/process gas thermal reaction mixed part, so that the acid gas is divided into front flow dividing acid gas and rear flow dividing acid gas;
3) the front shunting acid gas obtained in the step 2) is fully combusted with combustion air through a combustor of an acid gas/process gas thermal reaction mixing part, then enters a reaction furnace, and is mixed with the rear shunting acid gas in a mixing and strengthening facility;
4) cooling the process gas generated in the step 3) after the high-temperature thermal reaction by a condenser of a process gas condensing/preheating part to separate sulfur generated in the thermal reaction process, heating the process gas to the temperature of the catalytic reaction by a preheater, and then feeding the process gas into a catalytic reactor of a catalytic reaction part for reaction;
the catalytic reactor comprises two or more stages, the reaction product of the previous stage catalytic reactor is cooled by a condenser, the generated sulfur is separated out, the sulfur is preheated and enters the next stage catalytic reactor for reaction, and the process gas after the reaction of the last stage catalytic reactor enters the subsequent treatment stage through condensation.
According to the invention, the temperature of the sulfur recovery acid gas feed is 40-60 ℃, the pressure is 60-100KPaG, and the main component is H 2 S、CO 2 、H 2 O and amine solution, NH 3 And hydrocarbons, etc., wherein H 2 The concentration of S is preferably 15 to 50 mol%.
According to the invention, a control module in the shunting proportion calculation control device firstly determines a preliminary shunting proportion according to the concentration of the acid gas and the combustion temperature at the guaranteed lowest temperature, compares the theoretically calculated combustion temperature with the actual temperature of the reaction furnace, determines the influence of impurity components, feeds back the shunting proportion under the condition according to the feedback condition, and outputs the shunting proportion to the regulating valve control system.
Preferably, the front-split acid gas accounts for 40-100wt% of the purified acid gas.
Generally, the temperature of the front zone of the reaction furnace is 950-.
In the invention, the condenser can recover the heat of the process gas through the coolant according to the temperature of the process gas at the thermal reaction outlet, so as to cool down the elemental sulfur in the process gas, the liquid sulfur automatically flows into the product treatment process, and the outlet temperature of the condenser is 180 ℃.
The preheater heats the process gas according to the temperature required by the subsequent catalytic reaction. Preferably, the catalytic reactor comprises two stages, wherein the inlet temperature of the first-stage catalytic reactor is 250-280 ℃, the outlet temperature of the first-stage catalytic reactor is 300-330 ℃, the inlet temperature of the second-stage catalytic reactor is 200-250 ℃, and the outlet temperature of the second-stage catalytic reactor is 220-240 ℃.
According to the present invention, the above-described claus split sulphur recovery process can be achieved by means of the claus split sulphur recovery system.
The process parameters of the system components or all the system components which are not limited in the invention can be selected conventionally according to the prior art, and belong to the conventional technical means.
The present invention will be described in detail by way of examples.
Examples
This example illustrates the Claus split sulfur recovery system and process of the present invention.
In this example, the properties of acid gas feed 11 are shown in Table 1.
TABLE 1
As shown in fig. 1, acid gas feed 11 enters acid gas separation facility 6 of acid gas separation section 1, where entrained free water and MDEA droplets are separated and enter acid gas separation section 2. The separated condensate 12 is H-containing 2 S and a small amount of MDEA acid water are pressurized to 0.6MPaG by an acid gas condensate pump 7 and sent out of the device.
In the acid gas flow dividing part 2, a flow dividing control module outputs a proportional signal 67.6 percent to a front flow dividing acid gas 14 control loop and 32.4 percent to a rear flow dividing acid gas 13 loop of the acid gas through acid gas composition on-line analysis data and calculation of the front zone temperature and the rear zone temperature of the reaction furnace, and the proportional signal enters an acid gas/process gas thermal reaction mixing part 3.
The front flow-splitting acid gas 14 and combustion air enter a combustor and a reaction furnace 8 to be mixed and combusted, and the flow of the combustion air is 18534.6Nm 3 H, temperature 95 ℃ and pressure 95 KPaG. The temperature in the front zone of the burner and the reactor 8 was 1062.2 ℃ and the temperature in the rear zone of the burner and the reactor 8 was 877 ℃. The diameter of the burner and the reactor 8 is 3100 mm. The temperature of the hot reaction process gas is 15 ℃, the temperature is 300 ℃, the pressure is 71.5KPaG, and the flow rate is 33429Nm 3 The composition is shown in Table 2, and the thermal reaction conversion is about 63.73%.
TABLE 2
| Components | H 2 S(mol％) | CO 2 (mol％) | CH 4 (mol％) | H 2 O(mol％) | H 2 (mol％) |
| Content (wt.) | 5.19 | 28.57 | 0 | 19.73 | 0.46 |
| Components | N 2 (mol％) | SO 2 (mol％) | CO(mol％) | Organic sulfur (mol%) | Others (mol%) |
| Content (wt.) | 40.2 | 2.76 | 0.8 | 0.57 | 1.72 |
The hot reaction process gas 15 is cooled to 150-170 ℃ by the condenser 9 of the process gas condensation/preheating part 4, then heated to 250-260 ℃ by the preheater 10, and the primary catalytic pre-process gas 16 enters the primary catalytic reactor of the catalytic reaction part 5. The process gas undergoes the Claus reaction and the organic sulfur hydrolysis reaction in the catalytic reactor, the temperature of the process gas 17 is raised to 300-320 ℃ after the first-stage catalysis, the pressure is 63.5KPaG, and the composition is shown in Table 3.
TABLE 3
| Components | H 2 S(mol％) | CO 2 (mol％) | CH4(mol％) | H 2 O(mol％) | H 2 (mol％) |
| Content (c) of | 1.78 | 29.71 | 0 | 23.87 | 0.47 |
| Components | N 2 (mol％) | SO 2 (mol％) | CO(mol％) | Organic sulfur (mol%) | Others (mol%) |
| Content (wt.) | 41.4 | 0.89 | 0.82 | 0.14 | 0.92 |
After the primary catalysis, the process gas 17 is cooled to 150 ℃ and 170 ℃ through the condenser 9, and sulfur steam in the process gas is condensed. The coolant 22 of the condenser 9 is low pressure boiler feed water at 104 c and 2.0MPaG, and the coolant return 23 is 0.35MPaG of saturated steam.
The process gas is heated to 210-220 ℃ by the preheater 10, and then the process gas 18 before the second-stage catalysis enters the second-stage catalytic reactor of the catalytic reaction part 5. The process gas undergoes a Claus reaction in the catalytic reactor, the temperature of the process gas 19 after the secondary catalysis is increased to 230-240 ℃, the pressure is 55.5KPaG, and the composition is shown in Table 4.
TABLE 4
| Components | H 2 S(mol％) | CO 2 (mol％) | CH 4 (mol％) | H 2 O(mol％) | H 2 (mol％) |
| Content (c) of | 0.58 | 30.06 | 0 | 25.39 | 0.47 |
| Components | N 2 (mol％) | SO 2 (mol％) | CO(mol％) | Organic sulfur (mol%) | Others (mol%) |
| Content (wt.) | 41.9 | 0.29 | 0.83 | 0.14 | 0.34 |
After the process gas 19 after the secondary catalysis is cooled to 130-150 ℃ through the condenser 9, the tail gas 20 enters a tail gas treatment part, and the flow rate of the tail gas 20 is 31979Nm 3 The composition is shown in Table 5. The liquid sulfur condensed out from the condenser 9 has a temperature of 21 ℃ and automatically flows into the liquid sulfur product treatment part.
TABLE 5
| Components | H 2 S(mol％) | CO 2 (mol％) | CH 4 (mol％) | H 2 O(mol％) | H 2 (mol％) |
| Content (wt.) | 0.59 | 30.15 | 0 | 25.39 | 0.48 |
| Components | N 2 (mol％) | SO 2 (mol％) | CO(mol％) | Organic sulfur (mol%) | Others (mol%) |
| Content (wt.) | 42 | 0.29 | 0.83 | 0.12 | 0.15 |
The preheater 10 adopts 3.5-4.2MpaG saturated steam as a heating medium, the steam flow is 2.97 tons/hour, and condensed water enters a condensed water pipe network.
The Claus split-flow sulfur recovery system and the process are adopted to carry out acid gas feeding treatment, and the sulfur recovery rate of the sulfur production part is 95.93%.
Comparative example 1
The same raw material acid gas feeding composition and flow, if a direct current process is adopted, the operation temperature of the combustor and the reaction furnace 8 is 870 ℃, the stable combustion cannot be realized, fuel gas is introduced to increase the temperature, and the fuel gas consumption is increased by 630Nm compared with the invention 3 At a combustion air flow rate of 21801Nm 3 The increase of the reaction time per hour is 17.4 percent compared with the invention. The flow rate of the thermal reaction process gas 15 is 39204Nm 3 /h，H 2 S content 5.36 mol%, SO 2 3.93 mol%, organic sulfur content 1.28 mol%, thermal reaction conversion rate 47.2%, sulfur tail gas composition as shown in Table 6, flow rate 38639Nm 3 The recovery rate of sulfur in the sulfur production part is 87.9 percent.
TABLE 6
| Components | H 2 S(mol％) | CO 2 (mol％) | CH 4 (mol％) | H 2 O(mol％) | H 2 (mol％) |
| Content (c) of | 1.22 | 26.6 | 0 | 25.14 | 0.78 |
| Components | N 2 (mol％) | SO 2 (mol％) | CO(mol％) | Organic sulfur (mol%) | Others (mol%) |
| Content (c) of | 42.4 | 0.61 | 1.43 | 0.62 | 1.2 |
Comparative example 2
The same raw acid gas feed composition and flow rate, such as by conventional split-flow process, can be achieved by operating the burner and reactor 8 at 1027 deg.C and the combustion air flow rate at 17349Nm 3 The process hot reaction process gas 15 flow rate is 34192Nm 3 /h，H 2 S content 8.72 mol%, SO 2 The content was 4.38 mol%, the organic sulfur content was 1.25 mol%, and the conversion of the thermal reaction portion was 37.5%. Sulfur tail gas composition is shown in Table 7, flow rate is 32882.5Nm 3 And h, the sulfur recovery rate of the sulfur production part is 92.8 percent. The reactor has carbon deposition problem, and the service life of the catalyst is shortened by more than 10 percent compared with the invention.
TABLE 7
| Components | H 2 S(mol％) | CO 2 (mol％) | CH 4 (mol％) | H 2 O(mol％) | H 2 (mol％) |
| Content (wt.) | 0.89 | 28.79 | 0 | 25.38 | 0.59 |
| Components | N 2 (mol％) | SO 2 (mol％) | CO(mol％) | Organic sulfur (mol%) | Others (mol%) |
| Content (wt.) | 41.19 | 0.45 | 1.32 | 0.38 | 1.01 |
Compared with the technical scheme and the comparative example, the method further highlights the advantages of high sulfur recovery rate, low energy consumption, difficult carbon deposition of equipment and the like. Specifically, the results are shown in Table 8.
TABLE 8
| Scheme(s) | The invention | Direct current process | Traditional split-flow process |
| Sulfur recovery ratio (%) | 95.93 | 87.9 | 92.8 |
| Conversion of thermal reaction (%) | 63.73 | 47.2 | 37.5 |
| Fuel gas consumption (Nm) 3 /h) | 0 | 630 | 0 |
| Combustion air flow rate (Nm) 3 /h) | 18535 | 21801 | 17349 |
| Thermal process gas flow (Nm) 3 /h) | 33429 | 39204 | 34192 |
| Investment in equipment | Is low with | High (a) | Is low in |
| Carbon deposition of catalyst | No carbon deposition | No carbon deposit | Easy carbon deposition |
| Catalyst life | Long and long | Long and long | Short length |
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the illustrated embodiments.
Claims (7)
1. A Claus split-flow sulfur recovery system is characterized by comprising an acid gas split-flow part, an acid gas/process gas thermal reaction mixing part, a process gas condensing/preheating part and a catalytic reaction part;
the acid gas outlet of the acid gas separating part is communicated with the acid gas inlet of the acid gas separating part, the front split acid gas outlet and the rear split acid gas outlet of the acid gas separating part are respectively communicated with the front split acid gas inlet and the rear split acid gas inlet of the acid gas/process gas thermal reaction mixing part, the thermal reaction process gas outlet of the acid gas/process gas thermal reaction mixing part is communicated with the thermal reaction process gas inlet of the process gas condensing/preheating part, the pre-catalytic process gas outlet of the process gas condensing/preheating part is communicated with the pre-catalytic process gas inlet of the catalytic reaction part, and the post-catalytic process gas inlet of the process gas condensing/preheating part is communicated with the post-catalytic process gas outlet of the catalytic reaction part;
according to the flowing direction of materials, the acid gas/process gas thermal reaction mixing part comprises a combustor, a reaction furnace and a mixing strengthening facility which are sequentially communicated, wherein a combustion air inlet and a front diversion acid gas inlet are formed in the combustor, the combustion air inlet is communicated with a combustion air pipeline, the front diversion acid gas inlet is communicated with a front diversion acid gas outlet of the acid gas diversion part, a rear diversion acid gas inlet and a thermal reaction process gas outlet are formed in the mixing strengthening facility, the rear diversion acid gas inlet is communicated with a rear diversion acid gas outlet of the acid gas diversion part, and the thermal reaction process gas outlet is communicated with a thermal reaction process gas inlet of the process gas condensation/preheating part;
the acid gas liquid separating part comprises an acid gas liquid separating facility and an acid gas condensate pump, an acid gas inlet of the acid gas liquid separating facility is communicated with a sulfur recovery acid gas feeding pipeline, an acid gas outlet of the acid gas liquid separating facility is communicated with an acid gas inlet of the acid gas liquid separating part, and a condensate outlet of the acid gas liquid separating facility is communicated with the acid gas condensate pipeline through the acid gas condensate pump;
the acid gas diversion part comprises a diversion proportion calculation control device, the diversion proportion calculation control device comprises a control module, an acid gas composition on-line analyzer, a front region temperature meter and a rear region temperature meter, the signal input end of the acid gas composition on-line analyzer is positioned on an acid gas outlet pipeline of the acid gas diversion facility, the signal input end of the front region temperature meter is positioned at the front region of a reaction furnace of the acid gas/process gas thermal reaction mixing part, the signal input end of the rear region temperature meter is positioned at the outlet of the reaction furnace, and the signal output end of the acid gas composition on-line analyzer, the signal output end of the front region temperature meter and the signal output end of the rear region temperature meter are respectively communicated with the signal inlet of the control module.
2. The Claus split sulfur recovery system of claim 1 wherein the process gas condensing/preheating section comprises a condenser and a preheater, the number of stages of the condenser and the preheater is matched with the number of stages of the catalytic reactor of the catalytic reaction part, the condenser is provided with a thermal reaction process gas inlet, a condensed process gas outlet and a catalyzed process gas inlet, the preheater is provided with a condensed process gas inlet and a pre-catalysis process gas outlet, the thermal reaction process gas inlet is communicated with the thermal reaction process gas outlet of the acid gas/process gas thermal reaction mixing part, the condensed process gas outlet is communicated with the condensed process gas inlet, the pre-catalysis process gas outlet is communicated with the pre-catalysis process gas inlet, and the post-catalysis process gas inlet is communicated with the post-catalysis process gas outlet.
3. The claus split-flow sulfur recovery system of claim 1, wherein the catalytic reaction section comprises two or more stages of catalytic reactors, wherein two or more catalysts are contained in the catalytic reactors, the catalyst bottom is provided with a support, the upper layer is provided with inert ceramic balls, and the catalytic reactor is provided with a pre-catalytic process gas inlet and a post-catalytic process gas outlet.
4. A claus split-stream sulphur recovery process utilising the claus split-stream sulphur recovery system according to any of claims 1-3, characterized in that the claus split-stream sulphur recovery process comprises the steps of:
1) feeding the sulfur recovered acid gas into an acid gas liquid separation part, separating impurities carried in the sulfur recovered acid gas into the acid gas liquid separation part through an acid gas liquid separation facility, and pressurizing and conveying separated condensate out of the device through an acid gas condensate pump;
2) step 1), the purified acid gas enters an acid gas diversion part, and a diversion proportion calculation control device of the acid gas diversion part controls the acid gas diversion proportion according to the acid gas composition and the front region temperature and the rear region temperature of a reaction furnace of the acid gas/process gas thermal reaction mixing part, so that the acid gas is divided into front diversion acid gas and rear diversion acid gas;
3) the front shunting acid gas obtained in the step 2) is fully combusted with combustion air through a combustor of an acid gas/process gas thermal reaction mixing part, then enters a reaction furnace, and is mixed with the rear shunting acid gas in a mixing and strengthening facility;
4) cooling the process gas generated in the step 3) after the high-temperature thermal reaction by a condenser of a process gas condensing/preheating part to separate sulfur generated in the thermal reaction process, heating the process gas to the temperature of the catalytic reaction by a preheater, and then feeding the process gas into a catalytic reactor of a catalytic reaction part for reaction;
the catalytic reactor comprises two or more stages, the reaction product of the former stage catalytic reactor is cooled by a condenser, the generated sulfur is separated out, the sulfur is preheated and enters the latter stage catalytic reactor for reaction, and the process gas after the reaction of the last stage catalytic reactor enters the subsequent treatment stage by condensation.
5. The Claus split sulfur recovery process of claim 4 wherein H is in the sulfur recovery acid gas feed 2 The concentration of S is 15-50 mol%; the pre-diversion acid gas accounts for 40-100wt% of the purified acid gas.
6. The Claus flow-dividing sulfur recovery process as claimed in claim 4, wherein the temperature of the front zone of the reaction furnace is 950-1300 ℃, the temperature of the rear zone is 700-980 ℃, the temperature of the process gas after the thermal reaction obtained by mixing with the enhanced mixing facility is 250-350 ℃, and the temperature of the outlet of the condenser is 130-180 ℃.
7. The Claus split-flow sulfur recovery process as claimed in claim 4, wherein the catalytic reactor comprises two stages, the inlet temperature of the first-stage catalytic reactor is 250-280 ℃, the outlet temperature is 300-330 ℃, the inlet temperature of the second-stage catalytic reactor is 200-250 ℃, and the outlet temperature is 220-240 ℃.
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| CN100475313C (en) * | 2007-02-13 | 2009-04-08 | 西安中宇软件科技有限责任公司 | Device for the recovery and diffluence of sulfur dioxide and the system and method thereof |
| US7658906B2 (en) * | 2008-02-28 | 2010-02-09 | Conocophillips Company | Sulfur recovery plant |
| US20110171115A1 (en) * | 2009-07-22 | 2011-07-14 | Kps Technology & Engineering Llc | Method and Consolidated Apparatus for Recovery of Sulfur from Acid Gases |
| CN201662729U (en) * | 2010-05-04 | 2010-12-01 | 中国石油集团工程设计有限责任公司 | Acid gas control device of Claus sulphur recycling device |
| CN103964400B (en) * | 2014-04-30 | 2015-12-30 | 上海倍能化工技术有限公司 | A kind of claus tail-gas clean-up technique |
| CN104528659B (en) * | 2014-12-17 | 2017-04-12 | 田晓良 | Sulfur recycling process for circularly treating low-concentration acidy gas by utilizing liquid sulfur |
| CN107601436A (en) * | 2017-11-10 | 2018-01-19 | 晋城天成化工有限公司 | The device of Recovered sulphur in a kind of tail gas |
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