CN107151721B - System and method for producing direct reduced iron by double reforming and conversion of Lurgi gasification gas - Google Patents
System and method for producing direct reduced iron by double reforming and conversion of Lurgi gasification gas Download PDFInfo
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 88
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 81
- 238000002309 gasification Methods 0.000 title claims abstract description 78
- 238000002407 reforming Methods 0.000 title claims abstract description 75
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 33
- 239000003245 coal Substances 0.000 claims abstract description 53
- 238000005262 decarbonization Methods 0.000 claims abstract description 48
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 46
- 230000023556 desulfurization Effects 0.000 claims abstract description 45
- 238000005406 washing Methods 0.000 claims abstract description 41
- 239000003034 coal gas Substances 0.000 claims abstract description 33
- 239000000428 dust Substances 0.000 claims abstract description 28
- 239000008188 pellet Substances 0.000 claims abstract description 14
- 239000000463 material Substances 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 263
- 238000006722 reduction reaction Methods 0.000 claims description 71
- 238000000034 method Methods 0.000 claims description 62
- 230000015572 biosynthetic process Effects 0.000 claims description 45
- 238000003786 synthesis reaction Methods 0.000 claims description 45
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 33
- 239000011593 sulfur Substances 0.000 claims description 33
- 229910052717 sulfur Inorganic materials 0.000 claims description 32
- 238000002485 combustion reaction Methods 0.000 claims description 23
- 239000003546 flue gas Substances 0.000 claims description 23
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 22
- 230000001105 regulatory effect Effects 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- 239000000446 fuel Substances 0.000 claims description 18
- 239000002994 raw material Substances 0.000 claims description 13
- 238000006057 reforming reaction Methods 0.000 claims description 13
- 239000002918 waste heat Substances 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 11
- 230000006835 compression Effects 0.000 claims description 11
- 238000007906 compression Methods 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 11
- 239000001301 oxygen Substances 0.000 claims description 11
- 229910052760 oxygen Inorganic materials 0.000 claims description 11
- 238000011084 recovery Methods 0.000 claims description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims description 8
- 239000003054 catalyst Substances 0.000 claims description 5
- 238000010793 Steam injection (oil industry) Methods 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 239000005864 Sulphur Substances 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 34
- 229910052742 iron Inorganic materials 0.000 abstract description 12
- 238000000746 purification Methods 0.000 abstract description 6
- 230000010354 integration Effects 0.000 abstract description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 16
- 239000003077 lignite Substances 0.000 description 13
- 229910052799 carbon Inorganic materials 0.000 description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 239000000203 mixture Substances 0.000 description 9
- 239000003345 natural gas Substances 0.000 description 8
- 230000009286 beneficial effect Effects 0.000 description 4
- 230000008021 deposition Effects 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 3
- 239000003830 anthracite Substances 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000000227 grinding Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000010079 rubber tapping Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007323 disproportionation reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 238000005200 wet scrubbing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0073—Selection or treatment of the reducing gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The invention provides a system and a method for producing direct reduced iron by double reforming and conversion of Lurgi gasification gas, wherein the system comprises a Lurgi gasification unit, a dust removal washing unit, a desulfurization and decarbonization unit, a reforming and conversion unit and a gas-based reduction unit which are connected in sequence. In the invention, coal gas generated by the Lurgi gasifier is introduced into a gas-based reduction shaft furnace for reduction of pellets after dust removal washing, desulfurization and decarbonization and reforming conversion, so as to obtain reduced metallic iron. The invention can realize the effective integration of coal gasification technology, gas conversion technology, gas purification technology and reduction unit technology by combining a fixed bed pressurized gasification furnace, a reforming conversion unit and a gas-based reduction unit, and provides a system and a method for producing direct reduced iron by using coal gas with higher material and energy utilization rate.
Description
Technical Field
The invention belongs to the technical field of direct reduced iron production, relates to a system and a method for producing direct reduced iron by double reforming and conversion of Lurgi gasification gas, and particularly relates to a system and a treatment method for producing direct reduced iron by combining coal gas produced by a Lurgi gasification furnace with a Midrex/PERED gas-based reduction unit.
Background
Direct Reduced Iron (DRI) refers to a process of reducing iron ore to sponge iron below the melting temperature. Compared with the traditional blast furnace ironmaking method, the method omits procedures such as coking, sintering and the like, and has the advantages of short flow, little pollution, low consumption, no influence of shortage of high-quality coking coal and the like. Meanwhile, the direct reduced iron has low content of sulfur, phosphorus, silicon and other harmful impurities, and is beneficial to smelting high-quality pure steel in an electric furnace.
Since the study of gas-based shaft furnace technology by Midrex technologies, inc. in 1936, the development of direct reduced iron technology has been over 80 years old. The direct reduced iron process commercialized abroad is Midrex, hyL, PERED, etc. The foreign direct reduced iron production mainly uses pellets prepared from natural gas and iron concentrate as raw materials, and the direct reduced iron is mainly produced by reducing iron ore in a shaft furnace based on the natural gas direct reduced iron technology.
China is a country with deficient natural gas resources, and the use of natural gas as a main raw material for gas-based direct reduction iron process gas is difficult, high in cost and hardly feasible from the economic aspect from the viewpoint of the yield and consumption prediction analysis of the natural gas in China at present and in the future. In China, the search of an inexpensive air source capable of replacing natural gas for producing direct reduced iron has important significance on the technical difficulty of attacking the gas-based direct reduced iron.
Based on the national conditions of rich coal and little gas in China, the coal chemical industry has long history of development in China, and almost all coal gas processes in the world have practical attempts in China, and the coal gas processes are relatively mature. The low-quality non-coking coal is adopted to produce coal gas for directly reducing iron, so that the gas source cost is greatly reduced, and a opportunity is provided for the gas-based shaft furnace technology to be applied in China. At present, coal gasification technologies are mainly divided into three types of fixed bed, fluidized bed and entrained flow. Fixed beds are classified into atmospheric gasification (e.g., UGI furnaces, which tend to be obsolete due to severe pollution) and pressurized gasification (e.g., lurgi furnaces with slag tapping and BGL furnaces with slag tapping).
Table 1 shows typical gas compositions for the Lurgi gasification technology. Compared with the fluidized bed or entrained flow technology, the fixed bed pressurizing technology can be suitable for the lump coal with the granularity range of 5mm to 50mm, and does not need complex coal grinding or coal preparation technology.
TABLE 1 typical gas composition for fixed bed coal gasification process
US 4205830 and US 4225340 both disclose a method and apparatus for producing direct reduced iron from coal gas by reacting coal, oxygen and steam in a coal gasifier, introducing the reducing gas into a shaft furnace, using a portion of the top gas as fuel, and recycling a portion of the top gas to remove CO 2 And then reheating and mixing with coal gas and entering the shaft furnace. Lime (CaO) is added to the gasifier for removal of sulfides. CH in the gas component given in the patent 4 The content is below 0.3%, and the high CH generated by the coal gasification of the treatment fixed bed is obvious 4 The coal gas with the content of about 8 percent is not applicable; and CaO is added into the coal gasification device, and cannot be addedThe ideal desulfurization effect is achieved, and the current gas discharge requirement is difficult to meet.
CN 203034041U discloses a system for producing gas by pulverized coal gasification and directly reducing metallurgy of a gas-based shaft furnace, which gives a basic flow from coal gasification, wet scrubbing, water gas shift, desulfurization and decarbonization to the reduction shaft furnace, but the patent does not give implementation details, and only has theoretical reference value; and the patent does not contemplate recycling of the reduced top gas, for a significant amount of CO/H after the reaction 2 It is obviously unsuitable to treat the top gas directly as flue gas.
CN 1141402C discloses a device for producing sponge iron by utilizing pressurized gasification of coal water slurry. The patent selects a Texaco furnace, and the Texaco furnace is communicated to a shaft furnace after being heated by gas conversion, NHD purification and two parallel heating furnaces. The method can be applied to coal with high sulfur content and can recover sulfur. However, the Texaco furnace has high investment and high gasification pressure compared with a fixed bed coal gasifier; and the method that the gas is heated by the heating furnace and then fed into the shaft furnace is adopted, so that CO gasification carburization reaction is easy to occur, and the furnace tube is damaged to cause bad results.
To sum up, the national conditions of rich coal and little gas in China make the development of the technology for producing direct reduced iron by using coal gas in China imperative. The selection of suitable coal gasification technology, gas conversion technology, gas purification technology and reduction shaft furnace technology, and the better integration of the technologies are the problems to be solved urgently.
Disclosure of Invention
The invention aims to solve the problems in the prior art and provide a system for producing direct reduced iron by double reforming and conversion of Lurgi gasification gas and a treatment method thereof. According to the invention, the fixed bed pressurized gasifier (Lurgi gasifier), the reforming conversion unit and the gas-based reduction shaft furnace are combined, so that the effective integration of coal gasification technology, gas conversion technology, gas purification technology and reduction shaft furnace technology can be realized, and the utilization efficiency of materials and energy sources in a direct reduction metallurgical system is improved.
To achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the invention provides a system for producing direct reduced iron by double reforming and converting of Lurgi gasification gas, which comprises a Lurgi gasification unit, a dust removal washing unit, a desulfurization and decarbonization unit, a reforming and conversion unit and a gas-based reduction unit which are connected in sequence.
In the invention, compared with a pulverized coal gasifier or a coal water slurry gasifier, the fixed bed pressurized gasifier (Lurgi coal gasifier) has the advantages of lower investment, stable operation and no need of a complex coal preparation system. Compared with the fluidized bed or entrained flow technology, the method can be suitable for the lump coal with the granularity range of 5mm to 50mm, and does not need complex coal grinding or coal preparation technology; CH in synthesis gas 4 The higher content, generally above 8%, is beneficial to increasing the carbon content of the reduced iron product in the production of direct reduced iron; and, through subsequent double integral conversion, H in the synthesis gas can be improved 2 And CO content, thereby improving the yield of reduced iron.
The following technical scheme is a preferred technical scheme of the invention, but is not a limitation of the technical scheme provided by the invention, and the technical purpose and beneficial effects of the invention can be better achieved and realized through the following technical scheme.
As a preferable technical scheme of the invention, the dust removing washing unit is a washing tower; the dust removal washing unit is used for removing dust and cooling the raw gas synthesized by the Lurgi gasifier, so that desulfurization and decarbonization are carried out with the subsequent steps.
As a preferable embodiment of the present invention, the desulfurization and decarbonization unit includes a desulfurization device and a decarbonization device.
The desulfurization device is a fine desulfurization device, and the decarbonization device is a partial decarbonization device, so that a small amount of CO is reserved in the purified gas 2 As a raw material with CH 4 Carrying out double finishing reaction; at the same time, the effect of reducing carbon emission can be achieved.
Preferably, the sulfur-containing material of the desulfurization and decarbonization unit is connected with a sulfur recovery unit, and the sulfur recovery unit adopts a Claus method and other methods to recover sulfur in the coal gas.
Preferably, a pressure regulating unit is arranged between the desulfurization and decarbonization unit and the reforming and converting unit, and the pressure regulating unit is used for recovering energy and reducing the pressure of the coal gas to meet the production requirement of the shaft furnace.
Preferably, the pressure regulating unit employs a turbine, typical but non-limiting examples of which are: steam turbines, but are not limited to steam turbines.
Preferably, the gas outlet of the pressure regulating unit is connected with the feed gas inlet of the reforming conversion unit and the fuel inlet of the reforming conversion unit. The pressure-reducing coal gas processed by the pressure-regulating unit is divided into two parts, wherein one part is used as raw gas to enter the reforming and converting unit for reforming and converting reaction, and the other part is used as fuel to be connected with a burner of the reforming and converting unit, and is used as fuel to be supplied to the reforming and converting unit when the vehicle is started or the top gas is not available.
As a preferable technical scheme of the invention, the reforming conversion unit is a double reforming converter.
Preferably, the reforming conversion unit comprises a steam injection device.
Wherein, the reforming conversion unit can be filled with an anti-carbon catalyst, so that on one hand, the problem that the common heating furnace is easy to generate CO disproportionation reaction to cause metal carbon penetration dust is avoided, and on the other hand, compared with the single steam reforming, the CO is improved 2 Utilization rate, CO reduction 2 And the discharge reduces the load of the decarburization device.
Preferably, the gas-based reduction unit is a Midrex reduction shaft furnace or a PERED reduction shaft furnace.
Preferably, the gas-based reduction unit is provided with a pellet inlet, a synthesis gas injection port, a top gas outlet and a reduced iron outlet.
As a preferred technical scheme of the invention, the system further comprises a top gas washing device and a top gas compression device, wherein a top gas outlet of the gas-based reduction unit is connected with a gas inlet of the top gas washing device, a gas outlet of the top gas washing device is respectively connected with a gas inlet of the top gas compression device and a fuel inlet of the reforming conversion unit, and a gas outlet of the top gas compression device is connected with a gas inlet of the desulfurization and decarbonization unit.
Namely, the top gas generated by the gas-based reduction unit is divided into two parts after being washed, one part is used as fuel of the reforming and converting unit, and the other part is compressed by the compression device and then mixed with the coal gas to enter the desulfurization and decarbonization unit for removing sulfur and carbon dioxide.
The invention recycles the top gas generated by the gas-based reduction unit and can optimally regulate H in the raw gas 2 And the CO content, improves the utilization efficiency of raw material gas.
Preferably, the combustion flue gas outlet of the reforming conversion unit is connected with a flue gas heat exchange system.
Preferably, the flue gas heat exchange system comprises a waste heat boiler and a combustion air preheater, which may be provided after the waste boiler, saving energy by increasing the combustion air temperature. And the steam outlet of the flue gas heat exchange system is respectively connected with the steam inlet of the reforming conversion unit and the steam inlet of the Lurgi gasifier. The heat in the combustion flue gas of the conversion unit is recovered to heat the boiler to generate hot steam for the Lurgi gasifier and the reforming conversion unit; at the same time, the compressed air is heated, providing hot air to the conversion unit.
In a second aspect, the present invention provides a method for processing the above system, the method comprising the steps of:
(1) Raw material coal is gasified with oxygen and water vapor in a Lurgi gasification unit to generate raw gas;
(2) The crude gas in the step (1) is subjected to dust removal and washing, and then desulfurization and decarbonization are carried out, so that purified gas is obtained;
(3) Carrying out double integral conversion reaction on the purified gas in the step (2) to generate synthesis gas;
(4) And (3) enabling the synthesis gas to enter a gas-based reduction unit to be in countercurrent contact with the added pellets, and carrying out reduction reaction to generate reduced iron.
More specifically, the method comprises the following steps:
(1) Raw material coal is gasified with oxygen and water vapor in a Lurgi gasifier to generate raw gas;
(2) The crude gas in the step (1) enters a dust removal washing unit for dust removal and washing, and then enters a desulfurization and decarbonization unit for desulfurization and decarbonization to obtain purified gas;
(3) The purified gas in the step (2) enters a reforming conversion unit to carry out double reforming reaction to generate highly reduced synthetic gas;
(4) And (3) enabling the synthesis gas to enter a gas-based reduction unit to be in countercurrent contact with the added pellets, and carrying out reduction reaction to generate reduced iron.
Wherein the raw coal in the step (1) is lump coal and/or crushed coal.
The gasification reaction temperature in the step (1) is 1000-1600 ℃, the operating pressure is 1 MPaG-3 MPaG, the temperature of the raw gas generated by the gasification reaction is 600-700 ℃, and the temperature of the raw gas is reduced to 200-350 ℃ after dust removal and washing.
As a preferable technical scheme of the invention, the molar content of CO in the raw gas generated by the gasification reaction in the step (1) is 15-25 percent, H 2 The molar content of (C) is 38% -41%, CH 4 The mol content of (C) is 7% -13%, CO 2 The molar content of (2) is 25% -32%.
As a preferable technical scheme of the invention, the desulfurization and decarbonization in the step (3) comprises a desulfurization process and a decarbonization process.
Preferably, the desulfurization process is such that the total sulfur content in the shifted gas is < 1mg/m 3 。
Preferably, the decarbonization process causes CO in the shifted gas 2 The molar content is reduced to 1 to 5 percent. The decarbonization device is a part of decarbonization, and the gas after passing through the decarbonization device contains a small amount of CO 2 As raw material and CH 4 Reforming reaction is carried out, and the part of CO is utilized 2 Reducing carbon emissions.
Preferably, the transformed coal gas in the step (3) is subjected to desulfurization and decarbonization, pressure regulation and double integral conversion.
Preferably, the pressure is regulated to a pressure of 0.2MPaG to 0.5MPaG, which is used to meet the production requirements of the gas-based reduction unit.
Preferably, the gas after pressure regulation is divided into two parts, one part is used as raw gas to participate in double reforming reaction, and the other part is used as fuel for double reforming reaction, and supplies heat for the reformer when the car is started or the top gas is not available.
Preferably, H in the synthesis gas of step (3) 2 The total molar content with CO is more than 90 percent.
Preferably, H in the synthesis gas of step (3) 2 The molar ratio of the catalyst to CO is 1.5-2.0.
Preferably, the synthesis gas temperature in step (3) is 800 to 950 ℃, for example 800 ℃, 820 ℃, 850 ℃, 880 ℃, 900 ℃, 920 ℃, 950 ℃, etc., but is not limited to the values listed, and other values not listed in the range are equally applicable.
Preferably, the pressure of the synthesis gas in step (3) is from 0.2MPaG to 0.5MPaG, for example, 0.2MPaG, 0.3MPaG, 0.4MPaG or 0.5MPaG, etc., but is not limited to the recited values, and other non-recited values within the range of values are equally applicable.
In the present invention, the reforming conversion reaction is a double reforming reaction, comprising:
CH 4 +CO 2 ＝2CO+2H 2
CH 4 +H 2 O＝CO+3H 2
as a preferable technical scheme of the invention, the combustion flue gas generated by the double integer conversion reaction in the step (3) is used as a heat source to exchange heat with a waste heat boiler and a combustion air preheater in a flue gas heat exchange system, water vapor generated by heating the waste heat boiler is returned to participate in the gasification reaction and the double integer conversion reaction, and preheated air generated by preheating the combustion air preheater participates in the combustion heat supply of top gas.
Preferably, the top gas generated in the reduction reaction in the step (4) is divided into two parts after being washed, one part participates in desulfurization and decarbonization after being compressed, and the other part is used as fuel for double integral conversion reaction to recover heat.
The invention has the beneficial effects that:
(1) Compared with a pulverized coal gasification or coal water slurry gasification furnace, the invention adopts the fixed bed pressurized gasification furnace (Lurgi gasification furnace), has lower investment, stable operation and no need of a complex coal preparation system.
(2) The invention uses the double reforming reformer to replace the common steam reformer, and can improve CO 2 The utilization rate reduces the load of the decarburization device and reduces the carbon emission.
(3) The method adopts the mode of circulating participation reaction after washing the top gas, thereby improving the utilization efficiency of the raw gas; the waste heat boiler and the combustion air preheater are arranged on the reforming reaction furnace, so that sensible heat of the flue gas is recovered, byproduct steam can be used for the coal gasification furnace and the reforming reaction furnace, and the utilization efficiency of materials and energy sources is improved.
(4) According to the invention, the Lurgi gasifier is combined with the coal gasification technology, the gas conversion technology, the gas purification technology and the gas-based reduction unit technology, so that the limitation of natural gas in the gas-based direct reduction method can be overcome, the yield of the direct reduced iron can be improved, and the production cost can be reduced.
Drawings
FIG. 1 is a schematic structural diagram of a system for producing direct reduced iron by double reforming and converting a Lurgi gasification gas according to example 1 of the present invention;
the device comprises a 1-Lurgi gasification unit, a 2-dust removal washing unit, a 3-desulfurization and decarbonization unit, a 4-pressure regulation unit, a 5-reforming conversion unit, a 6-gas-based reduction unit, a 7-top gas washing device, an 8-top gas compression device, a 9-flue gas heat exchange system and a 10-sulfur recovery unit.
Detailed Description
For better illustrating the present invention, the technical scheme of the present invention is convenient to understand, and the present invention is further described in detail below. The following examples are merely illustrative of the present invention and are not intended to represent or limit the scope of the invention as defined in the claims.
The invention provides a system for producing direct reduced iron by double reforming and converting of Lurgi gasification gas and a treatment method thereof, wherein the system comprises a Lurgi gasification unit 1, a dust removal washing unit 2, a desulfurization and decarbonization unit 3, a reforming and converting unit 5 and a gas-based reduction unit 6 which are connected in sequence.
The processing method comprises the following steps:
(1) Raw material coal is gasified with oxygen and water vapor in a Lurgi gasification unit 1 to generate raw gas;
(2) The crude gas in the step (1) is subjected to dust removal and washing, and then desulfurization and decarbonization are carried out, so that purified gas is obtained;
(3) Carrying out double integral conversion reaction on the purified gas in the step (2) to generate synthesis gas;
(4) And (3) enabling the synthesis gas to enter a gas-based reduction unit 6 to be in countercurrent contact with the added pellets, and carrying out reduction reaction to generate reduced iron.
The following are exemplary but non-limiting examples of the invention:
example 1:
the embodiment provides a system for producing direct reduced iron by double reforming and converting of Lurgi gasification gas and a treatment method thereof, and as shown in figure 1, the system comprises a Lurgi gasification unit 1, a dust removal washing unit 2, a desulfurization and decarbonization unit 3, a pressure regulating unit 4, a reforming and converting unit 5 and a gas-based reduction unit 6 which are connected in sequence; it also comprises a top gas washing device 7 and a top gas compression device 8.
Wherein the Lurgi gasification unit 1 is provided with a lump coal feeding device, a steam inlet and an oxygen inlet;
the dust removing and washing unit 2 is a washing tower;
the sulfur-containing material of the desulfurization and decarbonization unit 3 is connected with a sulfur recovery unit 10;
the pressure regulating unit 4 adopts a turbine, and an air outlet of the pressure regulating unit is connected with a raw material gas inlet of the reforming conversion unit 5 and a fuel inlet of the reforming conversion unit 5;
the reforming conversion unit 5 is a double reforming furnace, which includes a steam injection device; the combustion flue gas outlet of the reforming conversion unit 5 is connected with a flue gas heat exchange system 9; the flue gas heat exchange system 9 comprises a waste heat boiler and a combustion air preheater, and the water vapor outlet of the flue gas heat exchange system 9 is respectively connected with the water vapor inlet of the reforming and converting unit 5 and the water vapor inlet of the Lurgi gasification unit 1.
The reforming conversion unit 5 is filled with an anti-carbon catalyst.
The gas-based reduction unit 6 is a Midrex reduction shaft furnace provided with a pellet inlet, a synthesis gas injection port, a top gas outlet and a reduced iron outlet.
The top gas outlet of the gas-based reduction unit 6 is connected with the gas inlet of the top gas washing device 7, the gas outlet of the top gas washing device 7 is respectively connected with the gas inlet of the top gas compression device 8 and the fuel inlet of the reforming conversion unit 5, and the gas outlet of the top gas compression device 8 is connected with the gas inlet of the desulfurization and decarbonization unit 3.
Taking 100 ten thousand tons/year of direct reduced iron production as an example, the method for processing by adopting the system comprises the following steps:
(1) 62t/h of lignite is fed into the Lurgi gasification unit 1, 77t/h of steam and 11045Nm are fed into the Lurgi gasification furnace 1 3 The gasification reaction of brown coal, oxygen and water vapor in the Lurgi coal gasification unit 1 is carried out to generate raw gas, and the yield of the raw gas is 103132Nm 3 /h，H 2 The molar ratio of/CO is 1.7;
(2) The crude gas in the step (1) enters a dust removal washing unit 2 for dust removal and washing, and enters a desulfurization and decarbonization unit 3 for desulfurization and decarbonization treatment, so that the total sulfur content is reduced to 1mg/m 3 The following is a procedure for removing most of the CO 2 ，CO 2 Removing to 5%; the removed sulfur enters a sulfur recovery unit 10 to recover sulfur by a Claus method, and the annual sulfur recovery amount of lignite with the sulfur content of 2 percent is 1.0 ten thousand tons;
(3) 80237Nm of desulphurized and decarbonized gas 3 /H, where H 2 The +CO molar content is 82.2%, the pressure is regulated by the pressure regulating unit 4, the pressure of the 2MPaG coal gas is reduced to 0.3MPaG, and 11233Nm of the 2MPaG coal gas is reduced 3 The/h coal gas is used as fuel to provide heat energy for the reforming conversion unit 5 and heat the synthesis gas from low temperature to 900 ℃, and the rest coal gas is 69004Nm 3 And/h enters a reforming conversion unit 5 to carry out reforming conversion reaction, and CH in the synthesis gas is converted 4 Conversion to H 2 And CO, generate 83000Nm 3 Synthesis gas/H, wherein H 2 Molar ratio to CO of 1.7, H 2 The +CO molar content is 92.1 percent, which accords with the production requirement of Midrex shaft furnace;
(4) Step (3), the synthesis gas enters from the middle part of the gas-based reduction unit 6, and is in countercurrent contact with 188t/h pellets added from the upper part of the gas-based reduction unit 6 to carry out reduction reaction, so as to generate reduced metallic iron, and the production rate of the direct reduced iron of the gas-based reduction unit 6 is 125t/h; the top gas of the gas-based reduction unit 6 is used as a heat source to exchange heat with a waste heat boiler and a combustion air preheater in the flue gas heat exchange system 9, water vapor generated by heating the waste heat boiler returns to participate in gasification reaction and reforming conversion reaction, and preheated air generated by preheating the combustion air preheater participates in reforming conversion reaction; avoiding the waste of materials generated by the fact that the coal gas cannot reach higher conversion rate in one-time reaction in the gas-based reduction unit 6.
In this example, the temperature, pressure and gas composition of the raw gas, the desulphurised decarbonized purified gas and the reforming reaction synthesis gas produced in each reaction stage are shown in table 2.
TABLE 2 typical gas composition for Lurgi fixed bed coal gasification process
Compared with the common heating furnace, the purified gas is converted by double reforming, thus improving CH 4 The utilization rate increases the reduction degree of the synthesis gas and reduces the carbon deposition risk; through CH 4 And H is 2 O reacts to generate CO+H 2 The effective gas yield is improved by 34.7 percent, and the yield of the reduced iron can be increased by 43.4t/h.
The production of 100 ten thousand tons/year direct reduced iron with daily lignite feeding amount of about 1480 tons and 1 Lurgi gasification furnace with daily lignite feeding amount of 1700 tons can meet the requirements, and one start and one standby can be adopted in actual production.
Example 2:
the present embodiment provides a system for producing direct reduced iron by double reforming and converting of Lurgi gasification gas and a treatment method thereof, the system structure is the same as in embodiment 1, and the difference is that: the gas-based reduction unit 6 is a PERED reduction shaft furnace.
Taking 30 ten thousand tons/year of direct reduced iron production as an example, the method for processing by adopting the system comprises the following steps:
(1) Anthracite coal 14t/h was charged into the Lurgi gasification unit 1, and 26t/h steam and 5848Nm were fed into the Lurgi gasification furnace 1 3 The gasification reaction of the anthracite, oxygen and water vapor in the Lurgi coal gasification unit 1 is carried out to generate crude gas with the yield of 30940Nm 3 /h，H 2 The molar ratio of/CO is 1.7;
(2) The crude gas in the step (1) enters a dust removal washing unit 2 for dust removal and washing, and enters a desulfurization and decarbonization unit 3 for desulfurization and decarbonization treatment, so that the total sulfur content is reduced to 1mg/m 3 The following is a procedure for removing most of the CO 2 ，CO 2 Removing to 5%;
(3) 24071Nm of desulphurized and decarbonized gas 3 /H, where H 2 The +CO molar content is 82.2%, the pressure is regulated by the pressure regulating unit 4, the pressure of the 2MPaG coal gas is reduced to 0.3MPaG, and 3370Nm of the 2MPaG coal gas is reduced 3 The/h coal gas is used as fuel to provide heat energy for the reforming conversion unit 5, and the synthesis gas is heated to 900 ℃ from low temperature, and the rest coal gas is 20701Nm 3 And/h enters a reforming conversion unit 5 to carry out reforming conversion reaction, wherein CH 4 Conversion to H 2 And CO, generate 24900Nm 3 Synthesis gas/H, wherein H 2 Molar ratio to CO of 1.7, H 2 The +CO molar content is 92.1 percent, which meets the production requirement of PERED shaft furnace;
(4) And (3) allowing the synthesis gas to enter from the middle part of the gas-based reduction unit 6, and carrying out countercurrent contact with the pellets of 56.4t/h added from the upper part of the gas-based reduction unit 6 to carry out reduction reaction to generate reduced metal iron, wherein the production rate of the direct reduced iron of the gas-based reduction unit 6 is 37.5t/h.
In this example, the temperature, pressure and gas composition of the raw gas, the desulphurised decarbonized purified gas and the shift reaction synthesis gas produced in each reaction stage were the same as those in example 1.
Compared with the common heating furnace, the purified gas is converted by double reforming, thus improving CH 4 The utilization rate increases the reduction degree of the synthesis gas and reduces the carbon deposition risk; through CH 4 And H is 2 O reacts to generate CO+H 2 The effective gas yield is improved by 34.7 percent, and the yield of the reduced iron can be increased by 13.0t/h.
The daily anthracite charging amount for producing 30 ten thousand tons/year direct reduced iron is about 320 tons, 1 Lurgi gasification furnace with 360 tons of daily coal charging amount can meet the requirement, and one start and one standby can be adopted in actual production.
Example 3
This example provides a system for producing direct reduced iron by double reforming conversion of Lurgi gasification gas and a treatment method thereof, and the system structure is the same as in example 1.
Taking 150 ten thousand tons/year of direct reduced iron production as an example, the method for processing by adopting the system comprises the following steps:
(1) 94t/h of lignite is fed into the Lurgi gasification unit 1, and 116t/h of steam and 16772Nm are fed into the Lurgi gasification furnace 1 3 The gasification reaction of brown coal, oxygen and water vapor in the Lurgi coal gasification unit 1 is carried out to generate crude gas with the yield of 156604Nm 3 /h，H 2 The molar ratio of/CO is 1.7;
(2) The crude gas in the step (1) enters a dust removal washing unit 2 for dust removal and washing, and enters a desulfurization and decarbonization unit 3 for desulfurization and decarbonization treatment, so that the total sulfur content is reduced to 1mg/m 3 The following is a procedure for removing most of the CO 2 ，CO 2 Removing to 1%; the removed sulfur enters a sulfur recovery unit 10 to recover sulfur by a Claus method, and the annual sulfur recovery amount of lignite with the sulfur content of 2 percent is 1.5 ten thousand tons;
(3) 115574Nm of desulphurized and decarbonized gas 3 /H, where H 2 The +CO molar content is 85.7 percent, the pressure is regulated by the pressure regulating unit 4, the pressure of the 2MPaG coal gas is reduced to 0.5MPaG, and 18492Nm of the gas is reduced 3 The/h coal gas is used as fuel to provide heat energy for the reforming conversion unit 5 and heat the synthesis gas from low temperature to 950 ℃, and the rest coal gas is 97082Nm 3 And/h enters a reforming conversion unit 5 to carry out reforming conversion reaction, and CH in the synthesis gas is converted 4 Conversion to H 2 And CO, generate 125000Nm 3 Synthesis gas/H, wherein H 2 Molar ratio to CO of 2.0, H 2 The +CO molar content is 92.4 percent, which accords with the production requirement of Midrex shaft furnace;
(4) And (3) allowing the synthesis gas to enter from the middle part of the gas-based reduction unit 6, and carrying out countercurrent contact with 281t/h pellets added from the upper part of the gas-based reduction unit 6 to carry out reduction reaction to generate reduced metallic iron, wherein the production rate of the direct reduced iron of the gas-based reduction unit 6 is 187.5t/h.
In this example, the temperature, pressure and gas composition of the raw gas, the desulphurised decarbonized purified gas and the reforming reaction synthesis gas produced in each reaction stage are shown in Table 3.
TABLE 3 example 3 gas composition at each stage
Compared with the common heating furnace, the purified gas is converted by double reforming, thus improving CH 4 The utilization rate increases the reduction degree of the synthesis gas and reduces the carbon deposition risk; through CH 4 And H is 2 O reacts to generate CO+H 2 The effective gas yield is improved by 38.9 percent, and the yield of the reduced iron can be increased by 72.9t/h.
The production of 100 ten thousand tons/year direct reduced iron has about 2250 tons of brown coal daily, 2Lurgi gasifiers with 1300 tons of coal daily can meet the requirements, and two-start and one-standby can be adopted in actual production.
Example 4
The present embodiment provides a system for producing direct reduced iron by double reforming and converting of Lurgi gasification gas and a treatment method thereof, the system structure is the same as in embodiment 1, and the difference is that: the gas-based reduction unit 6 is a PERED reduction shaft furnace.
Taking 80 ten thousand tons/year of direct reduced iron production as an example, the method for processing by adopting the system comprises the following steps:
(1) Lignite 51t/h was fed into the Lurgi gasification unit 1, 62t/h steam and 8990Nm were fed into the Lurgi gasification furnace 1 3 The gasification reaction of brown coal, oxygen and water vapor in the Lurgi coal gasification unit 1 is carried out to generate crude gas with the yield of 83929Nm 3 /h，H 2 The molar ratio of/CO is 1.7;
(2) The crude gas in the step (1) enters a dust removal washing unit 2 for dust removal and washing,enters a desulfurization and decarbonization unit 3 to carry out desulfurization and decarbonization treatment to reduce the total sulfur content to 1mg/m 3 The following is a procedure for removing most of the CO 2 ，CO 2 Removing to 3%; the removed sulfur enters a sulfur recovery unit 10 to recover sulfur by a Claus method, and the annual sulfur recovery amount of lignite with the sulfur content of 2% is 0.8 ten thousand tons;
(3) Desulfurizing decarbonizing gas 63618Nm 3 /H, where H 2 The +CO molar content is 83.9%, the pressure is regulated by the pressure regulating unit 4, the pressure of the 2MPaG coal gas is reduced to 0.2MPaG, and 10179Nm of the 2MPaG coal gas is reduced 3 The coal gas/h is used as fuel to provide heat energy for the reforming conversion unit 5 and heat the synthesis gas from low temperature to 800 ℃, and the rest coal gas 53440Nm 3 And/h enters a reforming conversion unit 5 to carry out reforming conversion reaction, and CH in the synthesis gas is converted 4 Conversion to H 2 And CO, generate 66700Nm 3 Synthesis gas/H, wherein H 2 Molar ratio to CO of 1.9, H 2 The +CO molar content is 91 percent, which meets the production requirement of PERED shaft furnace;
(4) And (3) allowing the synthesis gas to enter from the middle part of the gas-based reduction unit 6, and carrying out countercurrent contact with 150t/h pellets added from the upper part of the gas-based reduction unit 6 to carry out reduction reaction to generate reduced metallic iron, wherein the production rate of direct reduced iron of the gas-based reduction unit 6 is 100t/h.
In this example, the temperature, pressure and gas composition of the raw gas, the desulphurised decarbonized purified gas and the reforming reaction synthesis gas produced in each reaction stage are shown in Table 4.
TABLE 4 example 4 gas composition at each stage
Compared with the common heating furnace, the purified gas is converted by double reforming, thus improving CH 4 The utilization rate increases the reduction degree of the synthesis gas and reduces the carbon deposition risk; through CH 4 And H is 2 O reacts to generate CO+H 2 The effective gas yield is improved by 35.6 percent, and the yield of the reduced iron can be increased by 35.6t/h.
The production of 80 ten thousand tons/year direct reduced iron has about 1210 tons of brown coal per day, 1 Lurgi gasification furnace with 1400 tons of coal per day can meet the requirement, and one-on-one-standby can be adopted in actual production.
It can be seen from the above embodiments that in the present invention, the limitation of natural gas in the gas-based direct reduction method can be overcome by adopting the combination of the Lurgi gasifier, the coal gasification technology, the gas conversion technology, the gas purification technology and the gas-based reduction unit technology, the yield of directly reduced iron can be improved, and the production cost can be reduced.
The applicant states that the detailed process equipment and process flows of the present invention are described by the above examples, but the present invention is not limited to, i.e., does not mean that the present invention must be practiced in dependence upon, the above detailed process equipment and process flows. It should be apparent to those skilled in the art that any modification of the present invention, equivalent substitution of raw materials for the product of the present invention, addition of auxiliary components, selection of specific modes, etc., falls within the scope of the present invention and the scope of disclosure.
Claims (18)
1. The system for producing the direct reduced iron by double reforming and conversion of the Lurgi gasification gas is characterized by comprising a Lurgi gasification unit (1), a dust removal washing unit (2), a desulfurization and decarbonization unit (3), a pressure regulating unit (4), a reforming and conversion unit (5), a gas-based reduction unit (6), a top gas washing device (7) and a top gas compression device (8) which are connected in sequence; the reforming conversion unit (5) is a double reforming furnace;
the gas outlet of the pressure regulating unit (4) is connected with the raw gas inlet of the reforming conversion unit (5) and the fuel inlet of the reforming conversion unit (5);
the top gas outlet of the gas-based reduction unit (6) is connected with the gas inlet of the top gas washing device (7), the gas outlet of the top gas washing device (7) is respectively connected with the gas inlet of the top gas compression device (8) and the fuel inlet of the reforming conversion unit (5), and the gas outlet of the top gas compression device (8) is connected with the gas inlet of the desulfurization and decarbonization unit (3);
the combustion flue gas outlet of the reforming conversion unit (5) is connected with a flue gas heat exchange system (9), the flue gas heat exchange system (9) comprises a waste heat boiler and a combustion air preheater, and the steam outlet of the flue gas heat exchange system (9) is respectively connected with the steam inlet of the reforming conversion unit (5) and the steam inlet of the Lurgi gasification unit (1);
the method for producing direct reduced iron using the system comprises the steps of:
(1) Raw material coal is gasified with oxygen and water vapor in a Lurgi gasification unit (1) to generate raw gas, wherein the molar content of CO in the raw gas generated by the gasification reaction is 15-25%, and H is 2 The molar content of (C) is 38% -41%, CH 4 The mol content of (C) is 7% -13%, CO 2 The molar content of (2) is 25% -32%;
(2) The crude gas in the step (1) is subjected to dust removal and washing, and then desulfurization and decarbonization are carried out, so that purified gas is obtained;
(3) Carrying out double integral conversion reaction on the purified coal gas in the step (2) to generate synthesis gas, wherein H in the synthesis gas 2 Total molar content with CO > 90%, H 2 The molar ratio of the catalyst to CO is 1.5-2.0; the combustion flue gas generated by the double full-turning reaction is used as a heat source to exchange heat with a waste heat boiler and a combustion air preheater in a flue gas heat exchange system (9), water vapor generated by heating the waste heat boiler returns to participate in the gasification reaction and the double full-turning reaction, and preheated air generated by preheating the combustion air preheater participates in the combustion heat supply of top gas;
(4) And (3) enabling the synthesis gas to enter a gas-based reduction unit (6) to be in countercurrent contact with the added pellets, and carrying out reduction reaction to generate reduced iron.
2. The system according to claim 1, characterized in that the dust removal washing unit (2) is a washing tower.
3. The system according to claim 1, characterized in that the desulfurization and decarbonization unit (3) comprises a desulfurization device and a decarbonization device.
4. The system according to claim 1, characterized in that the sulfur-containing material of the desulfurization and decarbonization unit (3) is connected to a sulfur recovery unit (10).
5. The system according to claim 1, characterized in that the pressure regulating unit (4) employs a turbine.
6. The system according to claim 1, characterized in that the reforming conversion unit (5) comprises steam injection means.
7. The system according to claim 1, characterized in that the gas-based reduction unit (6) is a Midrex reduction shaft furnace or a PERED reduction shaft furnace.
8. The system according to claim 1, characterized in that the gas-based reduction unit (6) is provided with a pellet inlet, a synthesis gas injection inlet, a top gas outlet and a reduced iron outlet.
9. A method of processing a system according to any one of claims 1-8, characterized in that the method comprises the steps of:
(1) Raw material coal is gasified with oxygen and water vapor in a Lurgi gasification unit (1) to generate raw gas, wherein the molar content of CO in the raw gas generated by the gasification reaction is 15-25%, and H is 2 The molar content of (C) is 38% -41%, CH 4 The mol content of (C) is 7% -13%, CO 2 The molar content of (2) is 25% -32%;
(2) The crude gas in the step (1) is subjected to dust removal and washing, and then desulfurization and decarbonization are carried out, so that purified gas is obtained;
(3) Carrying out double integral conversion reaction on the purified coal gas in the step (2) to generate synthesis gas, wherein H in the synthesis gas 2 Total molar content with CO > 90%, H 2 The molar ratio of the catalyst to CO is 1.5-2.0; the combustion flue gas generated by the double integral conversion reaction is used as a heat source to exchange heat with a waste heat boiler and a combustion air preheater in a flue gas heat exchange system (9), and water vapor generated by heating the waste heat boiler is returned to participate inGasification reaction and double full-conversion reaction, wherein the preheated air generated by preheating the combustion air preheater participates in top gas combustion heat supply;
(4) And (3) enabling the synthesis gas to enter a gas-based reduction unit (6) to be in countercurrent contact with the added pellets, and carrying out reduction reaction to generate reduced iron.
10. The process of claim 9, wherein the desulfurization and decarbonization in step (2) includes a desulfurization process and a decarbonization process.
11. The process according to claim 10, wherein the desulphurisation process results in a total sulphur content in the shifted gas of < 1mg/m 3 。
12. The process of claim 10, wherein the decarbonizing process causes CO in the shifted gas 2 The molar content is reduced to 1 to 5 percent.
13. The process of claim 9, wherein the purified gas of step (3) is subjected to pressure regulation and then subjected to double reforming reaction.
14. The process of claim 13, wherein the pressure is adjusted to a pressure of 0.2mpa g to 0.5mpa g.
15. The process of claim 13, wherein the pressure-regulated gas is divided into two parts, one part being a feed gas to participate in the double reforming reaction and the other part being a fuel for the double reforming reaction.
16. The process of claim 9 wherein the synthesis gas temperature of step (3) is 800 ℃ to 950 ℃.
17. The process of claim 9, wherein the synthesis gas in step (3) has a pressure of from 0.2mpa g to 0.5mpa g.
18. The process of claim 9, wherein the top gas produced by the reduction reaction in step (4) is separated into two parts after washing, one part is compressed and returned as a reaction raw material for desulfurization and decarbonization, and the other part is used as fuel for double full-rotation reaction to recover heat.
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