CN117303312A - A method for producing ammonia synthesis gas from water gas shift gas - Google Patents
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Abstract
本申请涉及水煤气变换气技术领域，具体公开了一种水煤气变换气制造氨合成气方法，包括如下工序步骤：将碎煤加压气化得到粗煤气，将粗煤气依次经过变换反应、气体脱硫净化、压缩及氨合成工序后，得到氨合成气产品；所述变换反应包括：第一段变换反应和第二段变换反应，所述第一段变换反应温度为180‑300℃；所述第二段变换反应温度为200‑400℃；所述变换反应用催化剂为Co‑Mo系催化剂、反应压力为2.85‑3.00MPa、反应空速为5000‑7000h‑1、反应汽气比为0.50‑0.60，通过调节各个参数，使得变换后CO含量（干基，V%）最低4.05%，变换率最高84.42%，显著提高了变换反应的效率。This application relates to the technical field of water-gas-shifted gas, and specifically discloses a method for producing ammonia synthesis gas from water-gas-shifted gas, which includes the following steps: pressurizing and gasifying crushed coal to obtain crude coal gas, and subjecting the crude gas to sequential transformation reactions, gas desulfurization and purification , compression and ammonia synthesis process, an ammonia synthesis gas product is obtained; the shift reaction includes: a first stage shift reaction and a second stage shift reaction, the first stage shift reaction temperature is 180-300°C; the second stage shift reaction The stage shift reaction temperature is 200-400°C; the catalyst for the shift reaction is a Co-Mo series catalyst, the reaction pressure is 2.85-3.00MPa, the reaction space velocity is 5000-7000h -1 , and the reaction steam-to-gas ratio is 0.50-0.60. By adjusting various parameters, the post-conversion CO content (dry basis, V%) is as low as 4.05% and the conversion rate is as high as 84.42%, which significantly improves the efficiency of the conversion reaction.
Description
Technical Field
The present application relates to the field of water gas shift gas technology, and more specifically, to a method for producing ammonia synthesis gas from water gas shift gas.
Background
Water gas shift reaction (CO+H) 2 O=CO 2 +H 2 Water-gas-shift, WGS) is widely used in the preparation of ammonia, hydrogen, hydrocarbon and other products or in the regulation of CO content in urban natural gas. The water gas shift reaction is carried out under the action of a catalyst, the catalyst has high activity and good sulfur resistance, and active components of the catalyst are vulcanized, so that the problem of sulfur poisoning does not exist, sulfide in the shift raw material gas does not need to be removed in advance before the shift reaction, and the catalyst has the advantages of high operation flexibility, high activity, wide use temperature range, difficult poisoning, sulfur resistance and the like, can adapt to high-sulfur raw material gas, and has wide industrial application prospect.
However, the optimal activity and lifetime of the catalyst have a great relationship with the shift reaction conditions, so that the control of the process conditions of the shift reaction to promote the shift reaction is a problem to be solved.
Disclosure of Invention
In order to facilitate the shift reaction, the present application provides a process for producing ammonia synthesis gas from water gas shift gas.
A method for producing ammonia synthesis gas by water gas shift gas, comprising the following steps:
pressurizing and gasifying crushed coal to obtain crude gas, and sequentially carrying out the procedures of transformation reaction, gas desulfurization and purification, compression and ammonia synthesis on the crude gas to obtain an ammonia synthesis gas product;
the shift reaction includes: a first-stage conversion reaction and a second-stage conversion reaction, wherein the temperature of the first-stage conversion reaction is 180-300 ℃; the second stage of conversion reaction has a temperature of 200-400 ℃, the catalyst for conversion reaction is Co-Mo catalyst, the reaction pressure is 2.85-3.00MPa, and the reaction space velocity is 5000-7000h -1 The gas-gas ratio of the reaction is 0.50-0.60.
By adopting the technical scheme, the crushed coal is pressurized and gasified to obtain the crude gas, and the crude gas is subjected to the procedures of conversion reaction, gas desulfurization and purification, compression and ammonia synthesis in sequence to obtain an ammonia synthesis gas product;
the shift reaction mainly converts CO into H by the carbon monoxide shift reaction of the gasified raw gas 2 Co-Mo system usedThe sulfur-tolerant shift catalyst is suitable for the operation condition of higher sulfur content in the raw gas, has only minimum requirement (related to the content of CO in the raw gas, usually not lower than 500 ppm) on the sulfur in the raw gas, and has no upper limit, so that the raw gas does not need to be desulfurized and then shifted, and the process flow of the whole purification device is simpler; the Co-Mo sulfur-resistant wide temperature range conversion catalyst has no minimum water-gas ratio requirement, and saves steam consumption.
The raw gas entering the conversion reaction is in a saturated state, and the gas-gas ratio is 0.50-0.60, wherein the gas-gas ratio is the molar (or volume) ratio of water vapor and raw gas (dry) in the conversion raw gas. The gas-gas ratio in the shift gas is larger, the residual carbon monoxide component content is smaller, the balance shift rate of carbon monoxide can be improved, the carbon monoxide shift reaction is promoted, and the occurrence of side reactions (methanation, carbon precipitation and the like) can be restrained.
At a pressure of 2.85-3.00MPa and a space velocity of 5000-7000h -1 When the shift catalyst adsorbs reactant molecules at a high rate, the reactant molecules collide with the surface of the catalyst at a high probability, the reaction rate is high, the production reaction intensity of a unit catalyst is high, the catalyst treatment capacity is high, the carbon monoxide content of the first shift reaction is high, the catalyst reaction activity can be improved at the reaction temperature of 180-300 ℃, the shift chemical reaction rate in the initial stage of the reaction is favorably improved, the second shift reaction is performed, the reaction temperature of the second shift reaction is 200-400 ℃, the depth of carbon monoxide conversion is favorably improved at the temperature, the carbon monoxide content of the shift gas is reduced, and finally, the CO in the crude gas is subjected to the following reaction CO+H 2 O=CO 2 +H 2 Preparation of H 2 。
As preferable: the temperature of the first-stage shift reaction is 200-240 ℃.
The catalyst has a very important relation between the activity temperature range of the catalyst and the carbon monoxide shift reaction temperature, and the shift catalyst can cause sintering damage and deactivation of the catalyst under the condition of overhigh reaction temperature; in addition, too low a shift temperature may cause water vapor in the process gas to condense during the shift, thereby reducing the catalyst usage temperature and resulting in catalyst deactivation. The catalyst has higher catalytic activity in the initial stage of use, and the use temperature of the catalyst should be properly reduced; when the catalyst is used at the end stage or the activity is low, the use temperature of the catalyst should be properly increased so as to compensate the decrease of the catalyst activity and ensure the reaction rate of the carbon monoxide shift reaction.
By adopting the technical scheme, the temperature of the first-stage shift reaction is controlled to be 200-240 ℃, so that the activity of the catalyst can be further improved, and the shift reaction is promoted.
As preferable: the temperature of the second stage transformation reaction is 230-300 ℃.
By adopting the technical scheme, the temperature of the second-stage shift reaction is controlled to be 230-300 ℃, so that the activity of the catalyst can be further improved, and the shift reaction is promoted.
As preferable: the step of obtaining the raw gas through the crushed coal pressurized gasification further comprises a raw gas pretreatment step, wherein the pretreatment step comprises a step of heating the washed raw gas, and the heating temperature is 180-240 ℃.
By adopting the technical scheme, the crude gas is pretreated, dust and oil impurities contained in the crude gas are washed and separated through washing, and then the crude gas is heated to 180-240 ℃ to meet the activation temperature of a catalyst in the shift reaction, so that the shift reaction is promoted.
As preferable: the crude gas pretreatment step further comprises the step of filtering the crude gas after washing and heating, wherein the filtering step is to sequentially filter the crude gas after gravity sedimentation and cyclone separation.
By adopting the technical scheme, the shift catalyst can be protected from the poison of other impurities, large-particle impurities can be separated by gravity sedimentation, the sedimentation separation height is shortened, the separation effect is improved, and meanwhile, the abrasion of dust-containing airflow to internal parts is avoided; the cyclone separation can separate dust particles and oil (water) drops, and the pollution discharge can not influence the normal ventilation; the gas filter can separate impurities of smaller particle size.
As preferable: the first-stage shift reaction byproduct is medium-pressure saturated steam with the pressure of 1.2-1.6 MPa; the second stage transformation reaction by-product is low pressure saturated steam of 0.3-0.5 MPa.
By adopting the technical scheme, the medium-pressure saturated steam with the by-product of 1.2-1.6MPa of the shift gas at the outlet of the first-stage shift reaction furnace and the low-pressure saturated steam with the by-product of 0.3-0.5MPa of the shift gas at the outlet of the second-stage shift reaction furnace can improve the waste heat utilization efficiency of the saturated steam, wherein the medium-pressure steam can also be used as a heat source of the catalyst to ensure the activity temperature of the catalyst, so that the service life of the catalyst is prolonged.
As preferable: the volume density of the Co-Mo catalyst is 600-850kg/m 3 Specific surface area is more than or equal to 0.25cm 3 Per gram, the sulfur content is more than or equal to 100 mug/g.
By adopting the technical scheme, the volume density of the Co-Mo catalyst influences the filling degree and the hydrodynamic characteristics of the reactor. The volume density is 600-850kg/m 3 The filling degree of the catalyst can be improved, the number of active sites in the reactor is increased, the effective contact between the reactant and the catalyst is promoted, and the reaction efficiency is improved. Specific surface area is greater than or equal to 0.25cm 3 The/g provides more active sites for the reactants to adsorb and react, thereby increasing the reaction rate, promoting the interaction between reactant molecules, facilitating the reaction, and the sulfur content of the Co-Mo catalyst is very important for the shift reaction. Sulfides are active components of the catalyst and can provide the active sites and specific electronic structures required for the catalytic reaction. The sulfur content is more than or equal to 100 mug/g, so that the sulfide content on the surface of the catalyst can be increased, and the activity and selectivity of the catalyst are improved.
As preferable: the Co-Mo catalyst for the shift reaction is vulcanized and activated by taking nitrogen as a carrier and medium-pressure saturated steam as a heat source.
By adopting the technical scheme, nitrogen is used as a carrier, medium-pressure saturated steam from the first transformation reaction by-product provides a starting heat source for the catalyst, so that the catalyst is activated after being vulcanized, and the activity of the catalyst is improved.
In summary, the present application includes at least one of the following beneficial technical effects:
(1) According to the method, the temperature of the first-stage transformation reaction is controlled, so that the CO content (dry basis, V%) after the first-stage transformation reaction and the second-stage transformation reaction are respectively 11.05-11.33% and 4.37-4.46%, the transformation rates of the first-stage transformation reaction and the second-stage transformation reaction are respectively 56.41-57.50% and 82.83-83.19%, and the transformation reaction efficiency is improved.
(2) According to the method, the temperature of the second-stage transformation reaction is controlled, so that the CO content (dry basis, V%) after the first-stage transformation reaction and the second-stage transformation reaction are respectively 10.52-10.70% and 4.20-4.26%, the transformation rates of the first-stage transformation reaction and the second-stage transformation reaction are respectively 58.83-59.52% and 83.63-83.86%, and the transformation reaction efficiency is further improved.
(3) According to the method, the raw gas is pretreated before the transformation reaction, so that the transformed CO content (dry basis, V%) of the first-stage transformation reaction and the second-stage transformation reaction are 10.10.20-10.28 and 4.10-4.15 respectively, the highest transformation rate of the first-stage transformation reaction and the second-stage transformation reaction is 60.46-60.77% and 84.04-84.23%, respectively, and the transformation reaction efficiency is further improved.
(4) According to the method, after the crude gas is pretreated before the transformation reaction, the crude gas is filtered, so that the CO content (dry basis, V%) after the transformation reaction of the first section and the second section is respectively 10.15% and 4.05%, the highest transformation rate of the transformation reaction of the first section and the second section is respectively 60.96% and 84.42%, and the transformation reaction efficiency is further improved.
Through the steps, the parameters of the transformation process are regulated, so that the minimum CO content (dry basis, V%) after the transformation reaction of the first section and the second section is respectively 10.15 percent and 4.05 percent, the maximum transformation rate after the transformation reaction of the first section and the second section is respectively 60.96 percent and 84.42 percent, and the efficiency of the transformation reaction is obviously improved.
Detailed Description
The present application is described in further detail below in connection with specific examples.
The following raw materials are all commercial products, and are fully disclosed in the present application, and should not be construed as limiting the sources of the raw materials.
The method for preparing ammonia synthesis gas from water gas shift gas comprises the following steps: pressurizing and gasifying crushed coal to obtain crude gas, and sequentially carrying out the procedures of transformation reaction, gas desulfurization and purification, compression and ammonia synthesis on the crude gas to obtain an ammonia synthesis gas product;
wherein, the transformation reaction adopts a sulfur-tolerant transformation process to convert CO in the feed gas into H 2 The catalyst used for the shift is a sulfur tolerant shift catalyst. The device consists of a raw gas pretreatment unit, a reaction unit, a waste heat recovery and cooling unit and a catalyst heating and vulcanizing unit. (1) Raw gas pretreatment unit: the gas pretreatment system receives the raw gas sent by the coal gasification device. The unit is provided with a crude gas scrubber, a gas-gas heat exchanger, a gasified gas water pump, a circulating washing water pump and other devices. (2) A shift reaction unit: the transformation reaction unit is a core unit of the device. The crude gas from the upper unit sequentially passes through a gas filter, a first shift converter, a medium-pressure waste heat recoverer, a gas-gas heat exchanger, a second shift converter, low-pressure waste heat recovery gas and other devices in the unit. Wherein the first conversion furnace is vertical and has the specification of phi 3800 x-12600; the second converter is vertical and has the specification of phi 3800 x-12900. (3) Waste heat recovery and cooling unit: the waste heat recovery and cooling unit is provided with a precooler A, a precooler B, an intercooler, a final cooler, an ammonia washing tower and the like. (4) Catalyst temperature rising and vulcanizing unit: coO MoO is selected as Co-Mo series catalyst 3 /Al 2 O 3 To change catalyst, al 2 O 3 The catalyst is used as protective agent in an amount of 50-55m 3 。
The gas desulfurization and purification adopts a low-temperature methanol washing process, and H is removed under the pressure of 3.7MPa 2 S、COS、HCN、H 2 All impurities such as O, hydroxyl iron and the like, and the total sulfur in the purified gas can be less than 0.1ppm to obtain H 2 ；
Compression and ammonia synthesis process: the H obtained 2 The gas is sent into a tail gas compressor to be compressed to 0.188MPa (g), and is cooled after being heated to 147 ℃; after cooling to 40 ℃, the mixture is compressed again by a compressor, the pressure after compression is 0.4MPa, and the temperature is 30 ℃. The compressed hydrogen and nitrogen with the pressure of 2.5MPa are compressed to 6MPa together at 38 ℃, the temperature is increased to 400 ℃, ammonia is synthesized under the catalysis of a Habei-Boschmann catalyst under 10MPa, and then the product of the synthesized ammonia is obtained by cooling.
Examples
The process for making ammonia synthesis gas from the water gas shift gas of example 1 is as follows:
pressurizing and gasifying crushed coal to obtain crude gas, and generating crude gas with the CO dry basis content of about 26.00 (dry basis, V percent), wherein the gas-gas ratio of the crude gas is 0.50; the crude gas is reacted with Co-Mo catalyst under the pressure of 2.85MPa for 5000h -1 Under space velocity, obtaining shift gas H after the first stage shift reaction at 180 ℃ and the second stage shift reaction at 200 DEG C 2 Cooling the shift gas; the synthetic ammonia product is obtained through a low-temperature methanol washing process and a compression and ammonia synthesis process;
wherein, the composition (dry basis) of the raw gas is:
the bulk density of the Co-Mo catalyst was 750kg/m 3 Specific surface area is more than or equal to 0.25cm 3 Per gram, the sulfur content is more than or equal to 100 mug/g.
Examples 2 to 3
The process for producing ammonia synthesis gas from the water gas shift gas of examples 2-3 is the same as that of example 1, except that the shift reaction is at a different pressure, as shown in Table 1 in detail.
Examples 4 to 5
The process for making ammonia synthesis gas from the water gas shift gas of examples 4-5 is the same as example 2, except that the space velocity of the shift reaction is different, as detailed in Table 1.
Examples 6 to 7
The process for producing ammonia synthesis gas from the water gas shift gas of examples 6-7 is the same as that of example 4, except that the gas-to-gas ratio of the shift reaction is different, and is specifically shown in Table 1.
Table 1 examples 2-7 parameter tables for methods of producing ammonia synthesis gas from water gas shift gas
Examples 8 to 11
The process for producing ammonia synthesis gas from the water gas shift gas of examples 8-11 is the same as that of example 6, except that the temperature of the first stage shift reaction is different, as shown in Table 2 in detail.
Table 2 examples 8-11 parameter tables for methods of producing ammonia synthesis gas from water gas shift gas
Examples 12 to 15
The process for producing ammonia synthesis gas from water gas shift gas of examples 12-15 is the same as that of example 8, except that the temperature of the second stage shift reaction is different, as detailed in Table 3.
Table 3 examples 12-15 parameter tables for methods of producing ammonia synthesis gas from water gas shift gas
Examples 16 to 18
The process for producing ammonia synthesis gas from water gas shift gas of examples 16 to 18 is the same as that of example 13, except that the step of obtaining raw gas by pressurizing and gasifying raw coal further comprises a raw gas pretreatment step of heating the raw gas to 180 ℃, 210 ℃ and 240 ℃ after washing, and the remaining process steps are the same as those of example 11.
Examples
The method for producing ammonia synthesis gas by using the water gas shift gas of example 19 is the same as that of example 17, except that the raw gas further includes pretreatment and filtration, that is, the raw gas is sequentially subjected to gravity settling, cyclone separation and a gas filter of a hollow fiber filter material, and the rest of the method steps are the same as that of example 17.
Comparative example 1
The process for producing ammonia synthesis gas from water gas shift gas of comparative example 1 was the same as in example 1, except that the pressure of the shift reaction was 2.7MPa, and the remaining process steps were the same as in example 1.
Comparative example 2
The process for producing ammonia synthesis gas from water gas shift gas of comparative example 2 was the same as in example 1, except that the pressure of shift reaction was 3.1MPa, and the remaining process steps were the same as in example 1.
Comparative example 3
Comparative example 3A process for producing ammonia synthesis gas from a water gas shift gas was carried out in the same manner as in example 1, except that the space velocity of the shift reaction was 4500h -1 The remaining process steps are the same as in example 1.
Comparative example 4
Comparative example 4 the process for producing ammonia synthesis gas from water gas shift gas was the same as in example 1, except that the space velocity of the shift reaction was 7500h -1 The remaining process steps are the same as in example 1.
Comparative example 5
The process for producing ammonia synthesis gas from water gas shift gas of comparative example 5 was the same as in example 1, except that the gas-gas ratio of the shift reaction was 0.45, and the remaining process steps were the same as in example 1.
Comparative example 6
The process for producing ammonia synthesis gas from water gas shift gas of comparative example 6 was the same as in example 1, except that the gas-gas ratio of the shift reaction was 0.65, and the remaining process steps were the same as in example 1.
Comparative example 7
The process for producing ammonia synthesis gas from water gas shift gas of comparative example 7 was the same as in example 1, except that the temperature of the first stage shift reaction was 170 ℃, and the remaining process steps were the same as in example 1.
Comparative example 8
The process for producing ammonia synthesis gas from the water gas shift gas of comparative example 8 was the same as in example 1, except that the temperature of the first stage shift reaction was 310 ℃, and the remaining process steps were the same as in example 1.
Comparative example 9
The process for producing ammonia synthesis gas from water gas shift gas of comparative example 9 was the same as in example 1, except that the temperature of the second stage shift reaction was 180℃and the remaining process steps were the same as in example 1.
Comparative example 10
The process for producing ammonia synthesis gas from the water gas shift gas of comparative example 10 was the same as in example 1, except that the temperature of the second stage shift reaction was 420 ℃, and the remaining process steps were the same as in example 1.
Performance detection
The contents of CO at the outlets of the first stage shift reaction and the second stage shift reaction of the shift reactions of examples 1 to 19 and comparative examples 1 to 10 were calculated and the results are shown in Table 4 in detail.
The conversion rate refers to the conversion rate of CO calculated by the following formula: conversion rate of co= (CO feed amount-CO discharge amount)/CO feed amount; i.e. the conversion rate of the first stage conversion= (CO content in the raw gas-CO content after the first conversion)/CO content in the raw gas; conversion rate of the second-stage conversion= (CO content after the first conversion-CO content after the second conversion)/CO content after the first conversion.
TABLE 4 detection results for different examples and comparative examples
The detection results in table 4 show that the minimum CO content (dry basis, V%) after the transformation in the first stage and the second stage of the transformation process is 10.15% and 4.05%, respectively, and the maximum transformation rates in the first stage and the second stage are 60.96% and 84.42%, respectively, so that the transformation reaction efficiency is remarkably improved.
By combining the data of examples 1-3 and comparative examples 1-2, the CO content (dry basis, V%) after the transformation in the first and second stages of the transformation process of examples 1-3 is 12.43-12.92% and 4.83-4.99%, respectively, which is significantly lower than that of comparative examples 1-2, and the highest transformation rates in the first and second stages are 50.29-52.18% and 80.82-81.44%, respectively, which is significantly higher than that of comparative examples 1-2, respectively, indicating that the transformation reaction pressure is controlled to be 2.85-3.00MPa in the present application, which can improve the transformation reaction efficiency.
In combination with the data of examples 2, 4-5 and comparative examples 3-4, the transformed CO content (dry basis, V%) of the first and second stage of the transformation process of examples 2, 4-5 was 11.96-12.67% and 4.67-4.90%, respectively, which were significantly lower than those of comparative examples 3-4, the first and second stageThe conversion rates were 51.29-53.99% and 81.14-82.03%, respectively, which are significantly higher than those of comparative examples 3-4, indicating that the space velocity of the shift reaction was controlled to be 5000-7000h in the present application -1 The conversion reaction efficiency can be remarkably improved.
By combining the data of examples 4, 6-7 and comparative examples 5-6, the CO content (dry basis, V%) after the conversion of the first stage and the second stage of the conversion process of examples 4 and 6-7 is 11.55-12.17% and 4.53-4.74%, respectively, which is obviously lower than that of comparative examples 3-4, and the conversion rates of the first stage and the second stage are 53.19-55.59% and 81.77-82.56%, respectively, which is obviously higher than that of comparative examples 3-4, which shows that the gas-gas ratio of the conversion reaction is controlled to be 0.5-0.6 in the application, and the conversion reaction efficiency can be obviously improved.
In examples 6 and 8-11, the transformed CO content (dry basis, V%) of the first and second stage transformation of the transformation process of examples 8-10 is 11.05-11.33% and 4.37-4.46%, respectively, which are significantly lower than those of comparative examples 6 and 11, and the highest transformation rates of the first and second stages are 56.41-57.50% and 82.83-83.19%, respectively, which are both higher than those of examples 6 and 11, respectively, indicating that the temperature of the transformation reaction of the first stage is suitably controlled to 200-240 ℃, which can significantly improve the transformation reaction efficiency, possibly related to the temperature of the transformation reaction of the first stage, and the activity of the catalyst.
In examples 9 and 12-15, the transformed CO content (dry basis, V%) of the first and second stage transformation processes of examples 12-14 were 10.52-10.70% and 4.20-4.26%, respectively, which were significantly lower than those of comparative examples 9 and 15, and the highest transformation rates of the first and second stages were 58.83-59.52% and 83.63-83.86%, respectively, which were both higher than those of examples 9 and 15, indicating that the control of the temperature of the second stage transformation reaction was appropriate at 230-300 ℃, which significantly improved the transformation reaction efficiency, possibly related to the control of the temperature of the second stage transformation reaction, and improved the activity of the catalyst.
In examples 13 and 16-18, the transformed CO content (dry basis, V%) of the first and second stages of the transformation process of examples 16-18 is 10.20-10.28 and 4.10-4.15%, respectively, which is significantly lower than that of example 13, and the highest transformation rates of the first and second stages are 60.46-60.77% and 84.04-84.23%, respectively, which are both higher than that of example 13, indicating that the raw gas further includes pretreatment, particularly when the raw gas is washed and heated to 180-240 ℃, which significantly improves the transformation efficiency, possibly related to meeting the activation temperature of the catalyst in the transformation reaction after the pretreatment of the raw gas.
In examples 17 and 19, the CO content (dry basis, V%) after the first and second shift stages of the shift process of example 19 was 10.15% and 4.05%, respectively, which were significantly lower than that of example 17, and the maximum shift rates of the first and second stages were 60.96% and 84.42%, respectively, which were higher than that of example 17, respectively, indicating that the shift reaction efficiency was significantly improved when the raw gas was pretreated and then filtered, possibly in relation to the pretreatment and then filtered of the raw gas, and the shift catalyst was protected from poisoning by other impurities.
The present embodiment is merely illustrative of the present application and is not intended to be limiting, and those skilled in the art, after having read the present specification, may make modifications to the present embodiment without creative contribution as required, but is protected by patent laws within the scope of the claims of the present application.
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