US20160060553A1 - Reformed gas as fuel for primary reformer during startup - Google Patents

Reformed gas as fuel for primary reformer during startup Download PDF

Info

Publication number
US20160060553A1
US20160060553A1 US14/787,314 US201414787314A US2016060553A1 US 20160060553 A1 US20160060553 A1 US 20160060553A1 US 201414787314 A US201414787314 A US 201414787314A US 2016060553 A1 US2016060553 A1 US 2016060553A1
Authority
US
United States
Prior art keywords
reformed gas
total weight
water
gas
amount
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US14/787,314
Other languages
English (en)
Inventor
Shehzada Khurram
Ali Essa Alhammad
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Saudi Basic Industries Corp
Original Assignee
Saudi Basic Industries Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Saudi Basic Industries Corp filed Critical Saudi Basic Industries Corp
Priority to US14/787,314 priority Critical patent/US20160060553A1/en
Assigned to SAUDI BASIC INDUSTRIES CORPORATION reassignment SAUDI BASIC INDUSTRIES CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ALHAMMAD, Ali Essa, KHURRAM, Shezada
Publication of US20160060553A1 publication Critical patent/US20160060553A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/06—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by mixing with gases
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0495—Composition of the impurity the impurity being water
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/061—Methanol production
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1604—Starting up the process

Definitions

  • the invention satisfies these and other needs.
  • a method for recovery of a reformed gas produced in a methanol plant during startup is provided.
  • the method comprises decreasing the temperature of the methanol plant reactor reformed gas comprising (1) water in an amount no greater than 2.5 wt %, based on the total weight of the reformed gas, (2) methane in an amount that ranges from 1 wt % to 8 wt %, based on the total weight of the reformed gas, (3) hydrogen, (4) nitrogen, (5) carbon dioxide, and (6) carbon monoxide, to remove at least some of the water from the reformed gas; and using the water removed reformed gas as fuel in the methanol plant reactor.
  • FIG. 1 illustrates the conventional process.
  • FIG. 2 illustrates a version of the inventive process described herein.
  • Ranges can be expressed herein as from “about” one particular value, and/or to “about” another particular value. When such a range is expressed, a further aspect includes from the one particular value and/or to the other particular value. Similarly, when values are expressed as approximations, by use of the antecedent “about,” it will be understood that the particular value forms a further aspect. It will be further understood that the endpoints of each of the ranges are significant both in relation to the other endpoint, and independently of the other endpoint. It is also understood that there are a number of values disclosed herein, and that each value is also herein disclosed as “about” that particular value in addition to the value itself. For example, if the value “10” is disclosed, then “about 10” is also disclosed. It is also understood that each unit between two particular units are also disclosed. For example, if 10 and 15 are disclosed, then 11, 12, 13, and 14 are also disclosed.
  • references in the specification and concluding claims to parts by weight of a particular element or component in a composition denotes the weight relationship between the element or component and any other elements or components in the composition or article for which a part by weight is expressed.
  • X and Y are present at a weight ratio of 2:5, and are present in such ratio regardless of whether additional components are contained in the compound.
  • a weight percent (wt. %) of a component is based on the total weight of the formulation or composition in which the component is included.
  • the terms “optional” or “optionally” means that the subsequently described event or circumstance can or can not occur, and that the description includes instances where said event or circumstance occurs and instances where it does not.
  • compositions themselves to be used within the methods disclosed herein. These and other materials are disclosed herein, and it is understood that when combinations, subsets, interactions, groups, etc. of these materials are disclosed that while specific reference of each various individual and collective combinations and permutation of these compounds can not be explicitly disclosed, each is specifically contemplated and described herein. Thus, if there are a variety of additional steps that can be performed it is understood that each of these additional steps can be performed with any specific embodiment or combination of embodiments of the methods of the invention.
  • the present disclosure is directed towards a method for recovery of a reformed gas produced in a methanol plant during startup comprising: a) decreasing the temperature of the methanol plant reactor reformed gas comprising (1) water in an amount no greater than 2.5 wt %, based on the total weight of the reformed gas, (2) methane in an amount that ranges from 1 wt % to 8 wt %, based on the total weight of the reformed gas, (3) hydrogen, (4) nitrogen, (5) carbon dioxide, and (6) carbon monoxide, to remove at least some of the water from the reformed gas; and then b) using the water removed reformed gas as fuel in the methanol plant.
  • the recovery of the reformed gas can be used to increase the production and reduce the venting to have a positive impact on environment.
  • the recovery of the reformed gas can reduce the venting, reduce the waste, enhance the production, and/or reduce the carbon footprint.
  • the reformed gas is a mixture of purge gas and natural gas during standard methanol plant operation.
  • the natural gas can be used to start the reformer heating.
  • the reformed gas is recovered, rather than vented, during the startup.
  • the reformed gas is then used as fuel during the startup.
  • additional natural gas can be added to the reformed gas, if the reformed gas is not sufficient or if the heating value is not adequate.
  • the decreased temperature of the reformed gas ranges from 80° C. to 100° C., including exemplary values of 83° C., 85° C., 87° C., 90° C., 93° C., 95° C., and 97° C.
  • the temperature range can be derived from any two exemplary values.
  • the temperature of the reformed gas ranges from 83° C. to 97° C.
  • the temperature depends on the percentage of water in the reformed gas. In another aspect, the reformed gas temperature decreases to the point where the water can separate from the gas.
  • the time for startup ranges from 9 hours to 25 hours, including exemplary values of 10 hrs, 13 hrs, 15 hrs, 17 hrs, 20 hrs, and 23 hrs.
  • the time can be in a range derived from any two exemplary values.
  • the time for startup can range from 10 hrs to 25 hrs.
  • the reformed gas is cooled by passing through a heat exchanger.
  • the cooling can be performed with any cooling media depending on the required lowest temperature.
  • the required lowest temperature depends on the temperature at which the water can be separated from the gas.
  • the reformed gas is dried by passing through a separator. In one aspect, the reformed gas is further dried by passing through a filter.
  • the reformed gas comprises water, methane, hydrogen, nitrogen, carbon dioxide, and carbon monoxide. In another aspect, the reformed gas consists of water, methane, hydrogen, nitrogen, carbon dioxide, and carbon monoxide. In a yet further aspect, the reformed gas consists of methane, hydrogen, nitrogen, carbon dioxide, and carbon monoxide.
  • the reformed gas comprises hydrogen is present in an amount ranging from 50 wt % to 92.9 wt % hydrogen based on the total weight of the reformed gas; water is present in an amount ranging from 0 wt % to 2.5 wt % based on the total weight of the reformed gas; nitrogen is present in an amount ranging from 0.1 wt % to 5 wt % based on the total weight of the reformed gas; carbon monoxide is present in an amount ranging from 5 wt % to 20 wt % based on the total weight of the reformed gas; carbon dioxide is present in an amount ranging from 1 wt % to 15 wt % based on the total weight of the reformed gas; and methane is present in an amount ranging from 1 wt % to 8 wt % based on the total weight of the reformed gas.
  • the reformed gas comprises about 71.7 wt % hydrogen, about 2.5 wt % water, about 1.1 wt % nitrogen, about 14.3 wt % carbon monoxide, about 7.4 wt % carbon dioxide, and about 3 wt % methane.
  • the reformed gas comprises water in an amount no greater than 2.5 wt %, based on the total weight of the reformed gas. In a further aspect, the reformed gas comprises water in an amount ranging from 0 wt % to 2.5 wt %. In another aspect, the amount of water can be in a range derived from any two exemplary values. For example, the reformed gas comprises water in an amount ranging from 0 wt % to 2.0 wt %, or greater than 0 wt % to 2.0 wt %, or 0.3 wt % to 1.7 wt %.
  • the amount of water in the reformed gas is removed.
  • the amount of water can be in a range derived from any two exemplary values. For example, between 60% and 99% (or between 70% and 99%) of water in the reformed gas is removed.
  • removing water from the reformed gas comprises decreasing the temperature of the reformed gas and drying the cooled reformed gas.
  • the water is removed by using a heat exchanger, a separator, and/or a filter.
  • the water is a removed using any suitable method of absorption or adsorption.
  • the water removed reformed gas is cycled to a point before entry of natural gas in the methanol plant.
  • the method further comprises adding natural gas to the reformed gas after removing water.
  • the natural gas is added to the reformed gas in an amount ranging from 399,300 kg/25 hours of natural gas is added per about 1,339,307 kg/25 hours of reformed gas during plant startup.
  • the natural gas added depends on the heating value required. The amount of natural gas added above has been calculated based on the heat typically required for a methanol plant.
  • the total amount of natural gas saved by use of reformed gas as fuel is about 6132 MMNTU/25 hrs.
  • the amount of natural gas saved is calculated based on the typical methanol plant.
  • the reformed gas comprises hydrogen in an amount ranging from 50 wt % to 92.9 wt %.
  • the reformed gas can comprise hydrogen in an amount ranging from 55 wt % to 85 wt %, or 61 wt % to 74 wt %.
  • the reformed gas comprises methane in an amount that ranges from 1 wt % to 8 wt %, based on the total weight of the reformed gas.
  • the amount of methane is present in a range derived from any two exemplary values.
  • the reformed gas comprises methane in an amount that ranges from 1 wt % to 7 wt %, or 1.5 wt % to 5 wt %.
  • the reformed gas comprises methane in an amount of 3 wt %.
  • the reformed gas comprises nitrogen in an amount that ranges from 0.1 wt % to 5 wt %.
  • the range can be derived from any two exemplary values.
  • the reformed gas can comprise nitrogen in an amount that ranges from 2 wt % to 5 wt %.
  • the reformed gas comprises carbon dioxide in an amount that ranges from 1 wt % to 15 wt %. In further aspects can be in a range derived from any two exemplary values.
  • the reformed gas can comprise carbon dioxide in an amount that ranges from 6 wt % to 10 wt %.
  • the total impact of CO 2 is 900 to 1200 MT/25 hr, e.g., 1098 MT/25 hr. In one aspect, the total impact of CO 2 is calculated for the typical methanol plant. In another aspect, the total impact of CO 2 can change depending on the plant capacity.
  • the reformed gas comprises carbon monoxide in an amount that ranges from 5 wt % to 20 wt %. In further aspects can be in a range derived from any two exemplary values.
  • the reformed gas can comprise carbon monoxide in an amount that ranges from 6 wt % to 10 wt %.
  • the reformed gas heating value is 50,000 Kcal/Kg mol to 60,000 Kcal/Kg mol, e.g., 57,520 Kcal/Kg mol. In a further aspect, the reformed gas heating value is calculated for the typical methanol plant. In one aspect, the reformed gas heating value can vary from licensor to licensor.
  • the natural gas heating value is 180,000 Kcal/Kg mol to 200,000 Kcal/Kg mol, e.g., 192,930 Kcal/Kg mol. In one aspect, the natural gas heating value is calculated for the typical methanol plant and can vary depending on the plant.
  • the flow of reformed gas ranges from 18448 kg/hr to 84596 kg/hr. In further aspect, the flow can be in a range derived from any two exemplary values. For example, the flow of reformed gas can range from 19000 kg/hr to 80000 kg/hr.
  • the duty for the heat exchanger ranges from 4.2 ⁇ 10 6 KJ/hr to 6.5 ⁇ 10 6 KJ/hr and the amount of water removed from the reformed gas ranges from 55% to 98%. In one aspect, the duty for the heat exchanger ranges from 4.2 ⁇ 10 6 KJ/hr to 6.5 ⁇ 10 6 KJ/hr.
  • the duty can be in a range derived from any two exemplary values. For example, the duty for the heat exchanger ranges from 4.3 ⁇ 10 6 KJ/hr to 6.4 ⁇ 10 6 KJ/hr.
  • the present invention is directed towards an apparatus for recovery of a reformed gas comprising (1) water in an amount no greater than 2.5 wt %, based on the total weight of the reformed gas, (2) methane in an amount that ranges from 1 wt % to 8 wt %, based on the total weight of the reformed gas, (3) hydrogen, (4) nitrogen, (5) carbon dioxide, and (6) carbon monoxide, where the reformed gas is produced in a methanol plant during startup comprising: a closed loop line from a reformed gas flare stack line to a fuel line for the steam reformer, wherein the closed loop line comprises a heat exchanger, wherein the heat exchanger cools the reformed gas.
  • the apparatus is part of a methanol plant.
  • a methanol plant is a plant where methanol is produced from a raw material such as natural gas.
  • the reformed gas comprises water, methane, hydrogen, nitrogen, carbon dioxide, and carbon monoxide.
  • the reformed gas consists of water, methane, hydrogen, nitrogen, carbon dioxide, and carbon monoxide.
  • the reformed gas comprises hydrogen is present in an amount ranging from 50 wt % to 92.9 wt % hydrogen based on the total weight of the reformed gas; water is present in an amount ranging from 0 wt % to 2.5 wt % based on the total weight of the reformed gas; nitrogen is present in an amount ranging from 0.1 wt % to 5 wt % based on the total weight of the reformed gas; carbon monoxide is present in an amount ranging from 5 wt % to 20 wt % based on the total weight of the reformed gas; carbon dioxide is present in an amount ranging from 1 wt % to 15 wt % based on the total weight of the reformed gas;
  • the reformed gas consists of methane, hydrogen, nitrogen, carbon dioxide, and carbon monoxide.
  • the reformed gas comprises about 71.7 wt % hydrogen, about 2.5 wt % water, about 1.1 wt % nitrogen, about 14.3 wt % carbon monoxide, about 7.4 wt % carbon dioxide, and about 3 wt % methane.
  • the reformed gas composition has been calculated based on a typical methanol plant.
  • the reformed gas comprises water in an amount no greater than 2.5 wt %, based on the total weight of the reformed gas. In a further aspect, the reformed gas comprises water in an amount ranging from 0 wt % to 2.5 wt %, e.g., greater than 0 to 2.5 wt %. In another aspect, the amount of water can be in a range derived from any two exemplary values. For example, the reformed gas comprises water in an amount ranging from 0 wt % to 2.0 wt %, e.g., greater than 0 to 2.0 wt %, or 0.1 wt % to 1.8 wt %
  • the closed loop line cools and dries the reformed gas.
  • the heat exchanger reformed gas is cooled and is dried in a filter.
  • the loop line further comprises a separator and a filter wherein the separator, or the filter, or the combination thereof, removes 55% to 99% of the water from the reformed gas.
  • the amount of water in the reformed gas is removed.
  • the amount of water can be in a range derived from any two exemplary values. For example, between 60% and 90% of water in the reformed gas is removed.
  • the apparatus downstream of the heat exchanger, the apparatus further comprises a mixer, wherein the mixer adds natural gas to the reformed gas.
  • the natural gas is added to the reformed gas in an amount ranging from 399,300 kg/25 hours of natural gas is added per about 1,339,307 kg/25 hours of reformed gas during plant startup.
  • the amount of natural gas added depends on the required heating value. The above amount of natural gas is based on the typical methanol plant.
  • a reformed fuel gas 3 is a mixture of purge gas and natural gas from the natural gas line 1 .
  • Purge gas can come from a methanol separator 7 and from a vent scrubber 9 .
  • purge gas can flow to a steam reformer 3 and a hydrodesulphurization section 8 .
  • Natural gas can be added to the purge gas in order to provide the required heating value of the fuel gas for the reformer.
  • the reformed gas can be fed from a drain separator 4 to a methanol superconverter 5 through a compressor and no reformed gas goes to a flare stack 6 .
  • FIG. 2 an aspect of the new process is illustrated.
  • existing methanol reforming technology during conventional plant start-up, venting of enormous quantities of reformed gas would occur through a drain separator 23 to a flare stack 25 without a closed line loop comprising a heat exchanger 29 , a separator 30 and a coalescing filter 31 .
  • no purge gas is available for reformer/hydrodesulphurization section 27 and natural gas via natural gas line 20 is used to start reformer heating.
  • the disclosed process can recover the reformed gas produced in a methanol plant during startup and can use the reformed gas as fuel for a steam reformer 22 or as fuel for a package boiler 32 .
  • the venting temperature of the reformed gas can be around 80° C. to 100° C.
  • the reformed gas can contain at most 2.5 wt % water. Use of this gas as reformer fuel during startup can require reduction of temperature to remove water.
  • Exchanger 29 can reduce the temperature of the gas while separator 30 and coalescing filter 31 can remove water.
  • reformed gas can be fed to mixer 21 and steam reformer 22 .
  • the heating value of the reformed gas 23 can be low but can be supplemented with natural gas 20 if necessary. Accordingly, the process described above can utilize the reformed gas and has the following advantages: venting and waste are reduced while production and carbon footprint are enhanced.
  • the apparatus disclosed herein can use the inventive methods.
  • compositions and methods include at least the following aspects.
  • a method for recovery of a reformed gas produced in a methanol plant during startup comprising: (a) decreasing the temperature of the methanol plant reformed gas comprising (1) water in an amount no greater than 2.5 wt %, based on the total weight of the reformed gas, (2) methane in an amount that ranges from 1 wt % to 8 wt %, based on the total weight of the reformed gas, (3) hydrogen, (4) nitrogen, (5) carbon dioxide, and (6) carbon monoxide, to remove at least some of the water from the reformed gas; and (b) using the water removed reformed gas as fuel in the a steam reformer.
  • Aspect 2 The method of Aspect 1, wherein the reformed gas comprises hydrogen is present in an amount ranging from 50 wt % to 92.9 wt % hydrogen based on the total weight of the reformed gas; water is present in an amount ranging from 0 wt % to 2.5 wt % based on the total weight of the reformed gas; nitrogen is present in an amount ranging from 0.1 wt % to 5 wt % based on the total weight of the reformed gas; carbon monoxide is present in an amount ranging from 5 wt % to 20 wt % based on the total weight of the reformed gas; carbon dioxide is present in an amount ranging from 1 wt % to 15 wt % based on the total weight of the reformed gas; and methane is present in an amount ranging from 1 wt % to 8 wt % based on the total weight of the reformed gas.
  • Aspect 3 The method any one of Aspects 1-2, wherein the decreased temperature of the reformed gas is about 80° C. to 100° C.
  • Aspect 4 The method any one of Aspects 1-3, wherein from about 55% to about 99% of the water in the reformed gas is removed.
  • Aspect 5 The method any one of Aspects 1-4, wherein removing water from the reformed gas comprises decreasing the temperature of the reformed gas to cool the reformed gas and drying the cooled reformed gas.
  • Aspect 6 The method any one of Aspects 1-5, wherein the reformed gas is cooled by passing through a heat exchanger.
  • Aspect 7 The method any one of Aspects 1-6, wherein the reformed gas is dried by passing through a separator.
  • Aspect 8 The method any one of Aspects 1-7, wherein the reformed gas is further dried by passing through a filter.
  • Aspect 9 The method any one of Aspects 1-8, wherein the duty for the heat exchanger ranges from 4.2 ⁇ 10 6 KJ/hr to 6.5 ⁇ 10 6 KJ/hr and the amount of water removed from the reformed gas ranges from 55% to 99%.
  • Aspect 10 The method any one of Aspects 1-9, wherein the water removed reformed gas is recycled to a point before entry of natural gas in the methanol plant.
  • Aspect 11 The method any one of Aspects 1-10, further comprising adding natural gas to the reformed gas after removing water.
  • Aspect 12 The method any one of Aspects 1-11, wherein about 399,300 kg/25 hours of natural gas is added per about 1,339,307 kg/25 hours of reformed gas during plant startup.
  • Aspect 13 The method any one of Aspects 1-12, wherein the total amount of natural gas saved by use of reformed gas as fuel is about 6132 MMNTU/25 hrs.
  • Aspect 14 The method any one of Aspects 1-13 wherein flow of reformed gas is between about 18448 kg/hr and about 84596 kg/hr.
  • Aspect 15 An apparatus for recovery of a reformed gas comprising (1) water in an amount no greater than 2.5 wt %, based on the total weight of the reformed gas, (2) methane in an amount that ranges from 1 wt % to 8 wt %, based on the total weight of the reformed gas, (3) hydrogen, (4) nitrogen, (5) carbon dioxide, and (6) carbon monoxide, where the reformed gas is produced in a methanol plant during startup comprising: a closed loop line from a reformed gas flare stack line to a fuel line for a steam reformer; wherein the closed loop line comprises a heat exchanger; and wherein the heat exchanger cools the reformed gas.
  • Aspect 16 The apparatus of Aspect 15, wherein the closed loop line cools and dries the reformed gas.
  • Aspect 17 The apparatus any one of Aspects 15-16, wherein the loop line further comprises a separator and a filter wherein the separator, or the filter, or the combination thereof, removes from 55% to 99% of the water from the reformed gas.
  • Aspect 18 The apparatus according to Aspects 15-17, wherein downstream of the heat exchanger, the apparatus further comprises a mixer, wherein the mixer adds natural gas to the reformed gas.
  • Reformed gas Heating Value is 57520 Kcal/Kgmol; Natural gas: Heating Value is 192930 Kcal/Kgmol
  • Aspen Hysys-7.2 a chemical engineering tool is used for the calculations. As per the calculations the total natural gas saving is equivalent to 6132 MMBTU/25 hrs. Total reformed gas used in startup is 1339307 kg/25 hrs. Minimum and maximum flow of reformed gas is 18448 kg/hr and 84596 kg/hr respectively during startup. Total impact of CO 2 is 1098 MT/25 hr. Hydraulic calculations provide the size of the pipe. It is calculated that a 14′′ pipe with 40 schedule is appropriate to handle this flow rate.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)
US14/787,314 2013-05-06 2014-05-05 Reformed gas as fuel for primary reformer during startup Abandoned US20160060553A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US14/787,314 US20160060553A1 (en) 2013-05-06 2014-05-05 Reformed gas as fuel for primary reformer during startup

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US201361819735P 2013-05-06 2013-05-06
PCT/IB2014/061220 WO2014181243A1 (en) 2013-05-06 2014-05-05 Reformed gas as fuel for primary reformer during startup
US14/787,314 US20160060553A1 (en) 2013-05-06 2014-05-05 Reformed gas as fuel for primary reformer during startup

Publications (1)

Publication Number Publication Date
US20160060553A1 true US20160060553A1 (en) 2016-03-03

Family

ID=50841912

Family Applications (1)

Application Number Title Priority Date Filing Date
US14/787,314 Abandoned US20160060553A1 (en) 2013-05-06 2014-05-05 Reformed gas as fuel for primary reformer during startup

Country Status (4)

Country Link
US (1) US20160060553A1 (zh)
EP (1) EP2994416A1 (zh)
CN (1) CN105189343B (zh)
WO (1) WO2014181243A1 (zh)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10294102B2 (en) 2016-12-15 2019-05-21 Praxair Technology, Inc. Method of catalyst reduction in a hydrogen plant
TWI812713B (zh) * 2018-06-27 2023-08-21 丹麥商托普索公司 啟動加氫脫硫區段的方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4728506A (en) * 1986-05-16 1988-03-01 Catalyst Services, Inc. Start-up method for ammonia plants
US6818198B2 (en) * 2002-09-23 2004-11-16 Kellogg Brown & Root, Inc. Hydrogen enrichment scheme for autothermal reforming
CN101113127B (zh) * 2006-07-26 2010-05-12 李莉 一种以炼厂气为原料制取甲醇的方法
CN101823937B (zh) * 2010-05-11 2013-11-27 昆明理工大学 以冶金烟气中多碳源为原料一步法生产甲醇和二甲醚的方法
AU2013279683B2 (en) * 2012-06-19 2016-09-29 Haldor Topsoe A/S Process for reforming hydrocarbons and process for starting up a gas -to-liquid process
US9464237B2 (en) * 2012-09-05 2016-10-11 Haldor Topsoe A/S Method for starting-up a gas to liquid process

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
1400489 EP no *

Also Published As

Publication number Publication date
EP2994416A1 (en) 2016-03-16
CN105189343A (zh) 2015-12-23
CN105189343B (zh) 2017-06-09
WO2014181243A1 (en) 2014-11-13

Similar Documents

Publication Publication Date Title
US9943802B1 (en) Enhancement of claus tail gas treatment with membrane and reducing step
CN101835524A (zh) 从原料气中除去二氧化碳
US8388919B2 (en) Plant and process for removing carbon dioxide from gas streams
AU2007216457B2 (en) Refitting plants for acid gas removal
US20210220771A1 (en) Post-combustion co2 capture with heat recovery and integration
JP2013108108A (ja) 直接還元鉄製造システム
CN103079993A (zh) 从酸性气体中回收硫的方法和设备
JP2010201282A (ja) 揮発性有機化合物の回収方法及び回収装置
WO2013073663A1 (ja) 直接還元鉄製造システム
US20160060553A1 (en) Reformed gas as fuel for primary reformer during startup
EP3024563A2 (en) Split line system, method and process for co2 recovery
CN105764844A (zh) 硫回收单元和工艺
JP2013248608A (ja) Ｃｏ２分離システムのための統合ｃｏ２相変化吸収剤
US9884291B2 (en) Systems and methods for improved sulfur recovery from claus process tail gas
WO2012034921A1 (en) A process for the separation and capture of co2 from gas mixtures using amines solutions in anhydrous alcohols
KR20180137522A (ko) 이산화탄소 포획을 위해 용융 탄산염 연료 전지 애노드 배기를 후가공처리하는 방법
Olejnik et al. Utilitarian technological solutions to reduce CO2 emission in the aspect of sustainable development
US10376829B2 (en) Methods and systems for improving the energy efficiency of carbon dioxide capture
US9028682B2 (en) System and method for H2S removal integrated with stinson process CO2 removal
US8038779B2 (en) Methods and apparatus for reducing emissions in an integrated gasification combined cycle
JP5984776B2 (ja) 複合アミン吸収液、ｃｏ２又はｈ２ｓ又はその双方の除去装置及び方法
EP3672712B1 (en) Method and system for reclaiming amine absorption agent under controlled temperature.
US9708235B2 (en) Recycling gas to heat the hydrodesulphurization section
WO2013168588A1 (ja) 複合アミン吸収液、ｃｏ2又はｈ2ｓ又はその双方の除去装置及び方法
AU2016331718A1 (en) Absorbent liquid for CO2 and/or H2S, and apparatus and method using same

Legal Events

Date Code Title Description
AS Assignment

Owner name: SAUDI BASIC INDUSTRIES CORPORATION, SAUDI ARABIA

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:KHURRAM, SHEZADA;ALHAMMAD, ALI ESSA;SIGNING DATES FROM 20130830 TO 20130901;REEL/FRAME:036919/0593

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION