CN1844327A - Process for pretreatment of coke oven gas and partial oxidation preparation of synthetic raw gas - Google Patents
Process for pretreatment of coke oven gas and partial oxidation preparation of synthetic raw gas Download PDFInfo
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- CN1844327A CN1844327A CN 200610018740 CN200610018740A CN1844327A CN 1844327 A CN1844327 A CN 1844327A CN 200610018740 CN200610018740 CN 200610018740 CN 200610018740 A CN200610018740 A CN 200610018740A CN 1844327 A CN1844327 A CN 1844327A
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Abstract
The invention provides a technique for preparation of synthesis raw gases by pretreating coking gas and partial oxidation of coking gas and its devices to reach the purpose of producing large-scale synthesis ammonia and methanol device. The said technique mainly includes electrical tar collecting of coking gas, naphthalene-removing, deoxidation, desulfuration, pretreatment of coking gas, partial oxidation of coking gas, steam conversion and reaction heat utilization of reformed gases. The invention pretreats coking gas containing 20 %-30 % methane to get the coking gas, oxygen and water vapour to perform partial oxidation and steam conversion in converter according the purpose of synthesis raw gases by selecting oxidants with different components and reach a balance of selfheat. After the conversion reaction, the synthesis raw gases containing less than 0.5 % of methane content are obtained. The consumption of the coking gas reduces by 15 %-20 % compared with traditional conversion process, the consumption of the vapor reduces by 50 %-55 %, the investment reduces by 10 %-15 %, which can eliminate the discharge of the flue gas and protect the environment.
Description
Technical field
The present invention relates to the field of coke(oven)gas comprehensive utilization, be particularly related to a kind of with after coke(oven)gas process electrically trapped tar oil, coke oven qi exhaustion naphthalene, coke(oven)gas deoxidation, the coke oven gas desulfurization pre-treatment, produce the processing method and the key equipment thereof of synthetic raw gas again through purity oxygen or oxygen-rich air partial oxidation, with satisfy with coke(oven)gas be raw material large-scale synthetic ammonia or/and synthesizing methanol production to the synthetic raw gas requirement.
Background technology
Coke(oven)gas be coal under secluding air, the coke-oven gas that obtains after reclaiming through coke chemicals in the high-temperature coking process, the main compositing range of coke-oven gas is as follows.
Industry coke(oven)gas main ingredient
| Component | Content/% (volume) | Example 1 | Component | Content/% (volume) | Example 1 |
| CH 4 | 20～30 | 27.20 | C 2H 4 | 2～3 | 2.54 |
| CO | 5～13 | 6.50 | O 2 | 0.2～1.0 | 0.50 |
| CO 2 | 2～3 | 2.89 | Total sulfur gram/standard rice 3 | Relevant with sulfur-bearing in the coal | 5.53 |
| H 2 | 52～59 | 55.67 | Heavy hydrocarbon | Trace | |
| N 2 | 4～8 | 4.70 |
Because H in the coke(oven)gas
2+ CO content accounts for 60%～70%, CH
4Content accounts for 20%～30%, and unsaturated hydrocarbons accounts for 2%～3%, as adopts traditional steam reforming technology system synthetic raw gas not only to invest greatly, and for preventing that unsaturated hydrocarbons from analysing carbon and need adopt higher H
2The O/C mol ratio is generally 4.5～6, consumes a large amount of steam and fuel.The present invention has researched and developed the processing method of a kind of coke(oven)gas pre-treatment and partial oxidation preparation of synthetic raw gas for this reason, after coke(oven)gas process electrically trapped tar oil, coke oven qi exhaustion naphthalene, deoxidation and desulfurization pre-treatment, produce synthetic raw gas through coke(oven)gas partial oxidation and steam reforming again.According to the use difference of synthetic raw gas, select for use oxygen-rich air or pure oxygen as oxygenant, so that coke(oven)gas, oxygen, water vapor carry out partial oxidation reaction and steam reforming reaction, and reach autothermal equilibrium in converter.This method not only can be reduced investment outlay, and reduces floor space, also can eliminate the discharging that brings stack gas with other conversion process, the protection environment.
China does not also have large-scale synthetic ammonia (the 300000 tons of ammonia/years) device or the large-scale methyl alcohol (300,000 tons of methyl alcohol/years) of a kind of coke(oven)gas pre-treatment, pure oxygen partial oxidation preparation of synthetic raw gas to install in production and in service at present.
Summary of the invention
The object of the present invention is to provide a kind of processing method and key equipment, to satisfy the comprehensive utilization of large-scale synthetic ammonia installation or methanol device to coke(oven)gas economic worth and environment protection by coke(oven)gas pre-treatment and partial oxidation preparation of synthetic raw gas.It is few that this processing method has the production equipment floor space, and reduced investment and the coke(oven)gas that can adapt to various components change into the process of synthetic raw gas.
A kind of processing method that achieves the above object by coke(oven)gas pre-treatment and partial oxidation preparation of synthetic raw gas, it is characterized in that, this method is that the coke(oven)gas that will contain 20%-30% methane passes through earlier electrically trapped tar oil, coke oven qi exhaustion naphthalene, deoxidation and desulfurization pre-treatment in succession, and the tar content behind the control electrically trapped tar oil in the coke(oven)gas is less than 0.2 milligram/standard rice
3Behind the coke oven qi exhaustion naphthalene, the naphthalene content in the coke(oven)gas is less than 0.1PPM; After the coke(oven)gas deoxidation, the oxygen level in the coke(oven)gas is less than 10PPM; Behind the coke oven gas desulfurization, the total sulfur content in the coke(oven)gas is less than 0.1PPM; Produce synthetic raw gas through partial oxidation and steam reforming again, methane content in the synthetic raw gas is less than 0.5%, the waste heat of synthetic raw gas goes to reclaim, it is pure oxygen or oxygen-rich air that its partial oxidation is selected oxygenant for use, coke(oven)gas and oxygen and water vapor carry out partial oxidation and steam reforming reaction in same converter, the electrically trapped tar oil of coke(oven)gas, take off naphthalene, deoxidation and desulfurization pre-treatment are carried out respectively in multiple devices, the mol ratio of its coke(oven)gas and oxygen and water vapor in converter, with the heat release that the coke(oven)gas partial oxidation reaction produces carbonic acid gas and water vapor, carbonic acid gas that methane and oxidizing reaction produce and water vapor transform and generate CO+H
2Heat absorption, reach autothermal equilibrium metering.
Described coke(oven)gas in succession through electrically trapped tar oil, take off naphthalene, deoxidation and desulfurization pre-treatment after, after being preheating to 500～680 ℃, mixes coke(oven)gas with water vapor, control vapour/gas mol ratio is 0.9 ± 0.05, and its gas mixture is heated to 650 ± 30 ℃, enters converter through steam/coke(oven)gas preheater; After oxygen or oxygen-rich air are allocated 15% ± 5% protection steam into; be heated to 220 ± 20 ℃ through the oxygen preheat device, enter converter simultaneously, load conversion catalyst in the converter with the gas mixture of coke(oven)gas and water vapor; coke(oven)gas carries out partial oxidation and steam reforming reaction in converter after, CH
4Content reduce to below 0.5%, go out converter; The temperature of coming out from converter bottom reaches 970-1100 ℃ high temperature synthetic raw gas and enters the conversion waste heat boiler, the by-product middle pressure steam is personal, synthetic raw gas goes out to transform 700 ± 50 ℃ of the temperature of waste heat boiler, pressure is 30 ± 1 crust (bar), drops to 400 ± 20 ℃ through temperature after steam and the heat exchange of coke(oven)gas preheater again and goes to downstream synthetic ammonia or synthesizing methanol system.
The naphthalene agent is taken off in the CNA type absorption that the pre-treatment of described coke oven qi exhaustion naphthalene selects for use Sichuan Tianyi Science ﹠ Technology Co., Ltd to produce, and naphthalene agent major ingredient is taken off in its CAN absorption: activated carbon, Al
2O
3, 3～5 millimeters of granularity φ, bulk density: 500～900 kilograms/meter
3, use temperature: normal temperature～400 ℃
The DJ-1 type catalyzer deoxidation that described coke(oven)gas deoxidation pre-treatment selects for use Hubei Province's chemistry to be produced, DJ-1 dehydrogenation catalyst major ingredient: Al
2O
3, portions additive, 3～6 millimeters of granularity φ, bulk density: 700～800 kilograms/meter
3, 100～400 ℃ of use temperatures.
The low-temperature rectisol desulfurization is adopted in described coke oven gas desulfurization pre-treatment.
The conversion catalyst that described coke(oven)gas partial oxidation and steam reforming are adopted is the Z204/Z205/CN-20 catalyzer, 450 ℃ of this catalyzer initial activity temperature, anti-1600 ℃ of top temperature; Wherein Z204 is that southwestern chemical research institute produces product, and conversion catalyst is shaped as φ 19 * 19 * 9 mm rounds, major ingredient quality %:NiO 〉=14%, K
2O+Na
2O≤0.2%, Fe2O
3≤ 0.2%, CaO ≈ 10%, SiO
2≤ 0.2%, Al
2O
3≈ 55%, S≤0.01%, bulk density: 1160～1190 kilograms/meter
3, 450～1350 ℃ of use temperatures; Z205 is that southwestern chemical research institute produces product, and conversion catalyst is shaped as 10 millimeters ring-types of φ 25 * 17 * φ, major ingredient quality %:NiO6 ± 1%, K
2O+Na
2O≤0.2%, Fe
2O
3≈ 0.1%, CaO ≈ 3.5%, SiO
20.2%, Al
2O
3≈ 90%, bulk density: 1100～1150 kilograms/meter
3, use temperature＜1500 ℃; CN-20 is that southwestern chemical research institute produces product, and conversion catalyst is shaped as 19 * 9 * 19 millimeters ring-types of φ, major ingredient quality %:NaO 〉=14%, K
2O+Na
2O＜0.2%, Fe
2O
3≤ 0.2%, CaO6%, SiO
2≤ 0.2%, Al
2O
3≈ 76%, bulk density: 0.80 ± 0.05kg/L, use temperature＜1200 ℃.
Described coke(oven)gas conversion reaction steam/hydrocarbons ratio is not less than 2; Carbon ratio is 0.6～1.0, and better carbon ratio is 0.7 ± 0.02.
The coke(oven)gas electrically trapped tar oil, take off naphthalene, deoxidation and sweetening process and in some equipment, finish.Add pure oxygen or oxygen-rich air and water vapor in coke(oven)gas partial oxidation of the present invention and the steam reforming and in converter, react, do not need heat credit from the thermal transition equilibrium process.Whole process is divided into two stages.Fs is to carry out the combustion reactions of coke(oven)gas partial oxidation, produces carbonic acid gas and water vapor, and this reaction is a strong exothermic reaction.Subordinate phase is that carbonic acid gas and the water vapor that methane and oxygen combustion reactions produce carries out the endothermic conversion reaction, generates CO+H
2
The principal element that influences coke(oven)gas partial oxidation technology process has the activity of carbon ratio, steam/hydrocarbons ratio and conversion catalyst.Carbon ratio gets 0.6～1.0 usually, and the change carbon ratio is the effective means of regulating methane and carbon monoxide content in the reforming gas, control reaction temperature.In order to reduce the consumption of coke(oven)gas and oxygen, coke(oven)gas should be preheated to promptly 500～680 ℃ of comparatively high tempss as far as possible.Under this condition, the oxygen that adds 0.6～1.0 volume in a volume methane can reach the autothermal equilibrium process, has in fact ensured the abundant conversion of methane.For preventing that analysing carbon produces, consider oxygen consumption and available gas productive rate simultaneously in the conversion reaction, generally select for use steam/hydrocarbons ratio to be not less than 2.The activity of conversion catalyst is an important parameters, can quicken CO+H on the good catalyzer of selected activity
2Generative process, reduce remaining CH in the exit gas
4Amount, thus guarantee that methane content is less than 0.5% in the synthetic raw gas (reforming gas).
Used converter is a key equipment among the present invention, its structural shape and traditional secondary reformer are similar, be internal heat type partial oxidation furnace structural shape, the inner lining of furnace refractory materials, water jacket is established in the outside, and apparatus with catalyst inside, burner are equipped with the burner mixing burner that oxygenant and coke(oven)gas mixed firing are used, there are coke(oven)gas and mixture of steam import in converter top near burner mixing burner place, and reforming gas (synthetic raw gas) outlet is arranged at the converter bottom; Mixing burner is the key part of equipment, and it has to mix and prevents tempering, prevents that coke(oven)gas from analysing carbon, preventing that local superheating from burning out functions such as catalyzer when combustion air; When using oxygen-rich air, mixing burner is built-in multi-hole type, mixes burner as Switzerland's card Surrey formula burner when using pure oxygen, mixes with assurance oxygen, steam, coke(oven)gas, prevents that oxygen from bringing beds into, burns out catalyzer; Burner mixing burner is provided with entrance of cooling water, cooling water outlet, and oxidant inlet.
Advantage of the present invention is:
1, adopts the coke(oven)gas pre-treatment, earlier impurity such as the tar in the coke(oven)gas, naphthalene, oxygen and sulphur are taken off, obtain qualified coke oven unstripped gas to satisfy the requirement of technology coke(oven)gas partial oxidation reaction of the present invention;
2, adopt coke(oven)gas pre-treatment of the present invention and partial oxidation preparation of synthetic raw gas to produce the technology of synthetic ammonia, the coke(oven)gas consumption is about 1810 standard rices
3/ ton NH
3And traditional steam reforming need consume about 2000～2100 standard rices of coke(oven)gas
3/ ton NH
3, exceed processing method of the present invention more than 10%, major cause be about 30% coke(oven)gas as the burner fuel combustion, be used for the heating of boiler tube and loss;
3, converter is the structural shape that belongs to a kind of internal heat type partial oxidation furnace.It is abundant to have Btu utilization, and the characteristics that thermo-efficiency is high are under the quantitative condition in the coke(oven)gas supply especially, and a coke(oven)gas of should trying one's best uses as unstripped gas, reduces the consumption of non-technology usefulness gas.And use steam reforming technology, and temperature still can be discharged about 150 ℃ behind the flue gas process convection zone recovery waste heat, and the thermo-efficiency of converter is lower than 92%;
4, adopt reduced investment of the present invention.The tradition steam reforming but is built a chamber type one-stage converter without oxygen, comprises that tens of tons high-temperature alloy steel reformer tube overlaps 15000 standard rices with the present invention selected
3Compare/hour empty a branch, and the former investment still wants high;
5, adopt the present invention less, basic no waste discharge to the influence of environment.And when adopting traditional steam reforming technology, will discharge 3.266 * 10 every day
6Standard rice
3Flue gas (300,000 tons of ammonia/years), CO in the flue gas
2Be not fully utilized, and atmosphere is produced " greenhouse " effect, a spot of SO in the flue gas
2Also can produce detrimentally affect to plant environment;
6, the present invention and two sections steam reforming technologies of tradition are compared, and have coke(oven)gas and consume lowly, and steam consumption is economized, less investment, simple operation and other advantages.Coke(oven)gas consumption rate tradition conversion process lacks 15%～20%, and steam consumption lacks 50%～55%, and investment saves 10%～15%:
7, the production equipment that adopts the present invention to build, its processing unit are easy to make, construction is simple, production operation easily, device arranges compactly, has favorable economic benefit.
Description of drawings
Fig. 1 is the process flow diagram of coke(oven)gas pre-treatment of the present invention and partial oxidation preparation of synthetic raw gas;
Fig. 2 is the converter structural representation that adopts in the technology of the present invention.
Number in the figure title: 1, electrically trapped tar oil; 2, gas blower; 3, slightly take off the naphthalene groove; 4, feed gas compressor; 5, essence is taken off the naphthalene groove; 6, deoxygenator; 7, thionizer; 8, feed gas heater; 9, converter; 10, reforming gas boiler; 11, gas mixture interchanger; 12, drum; 13, oxygen preheat device; 14, catalyzer; 15, reforming gas (synthetic raw gas) outlet; 16, coke(oven)gas and mixture of steam import; 17, entrance of cooling water; 18, cooling water outlet; 19, oxidant inlet; 20, burner mixing burner.
Embodiment
Below by embodiment content of the present invention is described further.
Embodiment 1
What adopt the present invention's design is the 350000 tons of synthetic ammonia installation flow processs and the significant parameter of raw material with the coke(oven)gas.
The technical process explanation:
1, electrically trapped tar oil: the coke(oven)gas that comes from the battery limit (BL) takes off the tar the coke(oven)gas to less than 0.2PPM through electrical tar precipitator 1
2, coke oven qi exhaustion naphthalene: the coke(oven)gas behind electrically trapped tar oil boosts to 1.3bar (crust) by gas blower 2,40 ℃ of temperature, coke(oven)gas enters and slightly takes off naphthalene groove 3, the coke(oven)gas that slightly takes off behind the naphthalene is compressed to 3.1bar (crust) through feed gas compressor 4 one-levels, the coke(oven)gas of 160 ± 10 ℃ of temperature enters essence and takes off naphthalene groove 5 after the heat exchange, takes off behind the naphthalene naphthalene in the coke(oven)gas by 60 milligrams/standard rice through two-stage
3Reduce to below the 0.1PPm, coke(oven)gas returns feed gas compressor 4 after being cooled to normal temperature again.
3, coke(oven)gas deoxidation, desulfurization: take off the coke(oven)gas about 32.0bar of pressure (crust) after feed gas compressor 4 two, three grades of compressions behind the naphthalene, behind heat exchange to 250 ± 10 ℃, enter deaerator 6, oxygen level is reduced to below the 10PPm by 1%.
Coke(oven)gas after the deoxidation is again through heat exchange, and temperature drops to 10 ± 0.5 ℃, enters the gas that the further heat exchange of low-temperature rectisol desulphurization system cools to temperature-20 ± 0.5 ℃ and enters thionizer 7, the H in the gas
2Sulfur component such as S, COS is absorbed by methanol solution, and total sulfur content is less than 0.1PPm in the gas after the desulfurization, and processed gas goes to the partial oxidation system.
4, coke(oven)gas transforms: the coke(oven)gas after the desulfurization is preheating to 350 ± 20 ℃ of temperature through feed gas heater 8, then with the 4.0MPa vapor mixing, the vapour volume flow is 0.9 ± 0.02 times of coke(oven)gas volumetric flow rate, gas mixture through gas mixture interchanger 11 and reforming gas heat exchange, is heated to the burner mixing burner 20 of delivering to converter 9 after 660 ± 20 ℃ again; Oxygen from pipe network is preheating to 220 ± 20 ℃ of temperature through oxygen preheat device 13 earlier, enters the burner mixing burner 20 of converter 9 then.Oxygen, coke(oven)gas and steam carry out catalytic partial oxidation reaction and steam reforming reaction in the converter 9 of interior dress conversion catalyst 14, go out 1040 ± 50 ℃ of the reforming gas temperature of converter outlet 15, pyrolytic conversion gas produces middle pressure steam earlier in reforming gas boiler 10, temperature is reduced to 720 ± 20 ℃, and then through gas mixture interchanger 11 heating mixing raw material gas, the reforming gas temperature is reduced to about 370 ± 20 ℃ and is entered downstream synthetic ammonia or synthesizing methanol device systems.
The major equipment operating parameters:
1, converter: 4274 millimeters of external diameters, 3900 millimeters of internal diameters are high 19740 millimeters; Design pressure (a): in 3.4 MPas in the converter, chuck is normal pressure; Design temperature: 250 ℃ of housings, 100 ℃ of chucks; Working pressure (a): in 3.0 MPas in the converter, chuck is normal pressure; Service temperature ℃: the oxidizing fire district is 1655 ℃ in the converter, 1034 ℃ of converter outlet reforming gas temperature, 90 ℃ of jacket temperatures; Loaded catalyst: 19.3 meters of Z204 catalyzer
3, 6.43 meters of CN20 catalyzer
3, 6.43 meters of Z205 catalyzer
3
2, transform waste heat boiler: 2044 millimeters of stove diameters, long 7858 millimeters; Design pressure (g): tube side 3.6 MPas, shell side 4.6 MPas; Design temperature ℃: 400 ℃ of tube sides, 260 ℃ of shell sides; Working pressure (a): tube side 2.95 MPas, shell side 4.0 MPas; Service temperature ℃: 1034.1 ℃/706.7 ℃ of tube sides, 250.3 ℃ of shell sides, 138.3 meters of heat interchanging areas
2
Claims (9)
1, a kind of processing method by coke(oven)gas pre-treatment and partial oxidation preparation of synthetic raw gas, it is characterized in that, this method is that the coke(oven)gas that will contain 20%-30% methane passes through earlier electrically trapped tar oil, coke oven qi exhaustion naphthalene, deoxidation and desulfurization pre-treatment in succession, and the tar content behind the control electrically trapped tar oil in the coke(oven)gas is less than 0.2mg/Nm3; Behind the coke oven qi exhaustion naphthalene, the naphthalene content in the coke(oven)gas is less than 0.1PPM; After the coke(oven)gas deoxidation, the oxygen level in the coke(oven)gas is less than 10PPM; Behind the coke oven gas desulfurization, the total sulfur content in the coke(oven)gas is less than 0.1PPM; Produce synthetic raw gas through partial oxidation and steam reforming again, methane content in the synthetic raw gas is less than 0.5%, the waste heat of synthetic raw gas goes to reclaim, it is pure oxygen or oxygen-rich air that its partial oxidation is selected oxygenant for use, coke(oven)gas and oxygen and water vapor carry out partial oxidation and steam reforming reaction in same converter, the electrically trapped tar oil of coke(oven)gas, take off naphthalene, deoxidation and desulfurization pre-treatment are carried out respectively in multiple devices, the mol ratio of its coke(oven)gas and oxygen and water vapor in converter, with the heat release that the coke(oven)gas partial oxidation reaction produces carbonic acid gas and water vapor, carbonic acid gas that methane and oxidizing reaction produce and water vapor transform and generate CO+H
2Heat absorption, reach autothermal equilibrium metering.
2, according to the processing method of described coke(oven)gas pre-treatment of claim 1 and partial oxidation preparation of synthetic raw gas, it is characterized in that, coke(oven)gas in succession through electrically trapped tar oil, take off naphthalene, deoxidation and desulfurization pre-treatment after, after being preheating to 500～680 ℃, mixes coke(oven)gas with water vapor, control vapour/gas mol ratio is 0.9 ± 0.05, its charge heating to 650 ± 30 ℃ enter converter; Oxygen or oxygen-rich air are preheated to 220 ± 20 ℃ after allocating 15% ± 5% steam into, enter converter simultaneously with coke(oven)gas/water vapor mixture, load conversion catalyst in the converter, coke(oven)gas carries out partial oxidation and steam reforming reaction in converter after, and CH
4Content reduce to below 0.5%, go out converter; The temperature of coming out from converter bottom reaches 970-1100 ℃ high temperature synthetic raw gas and enters the conversion waste heat boiler, the by-product middle pressure steam is personal, synthetic raw gas goes out to transform 700 ± 50 ℃ of the temperature of waste heat boiler, pressure is 30 ± 1 crust, drops to 400 ± 20 ℃ through temperature after steam/coke(oven)gas preheater heat exchange again and goes to downstream synthetic ammonia or synthesizing methanol system.
3, according to the processing method of described coke(oven)gas pre-treatment of claim 1 and partial oxidation preparation of synthetic raw gas, it is characterized in that, the naphthalene agent is taken off in the CNA type absorption that the pre-treatment of described coke oven qi exhaustion naphthalene selects for use Sichuan Tianyi Science ﹠ Technology Co., Ltd to produce, and naphthalene agent major ingredient is taken off in its CAN absorption: activated carbon, Al
2O
3, 3～5 millimeters of granularity φ, bulk density: 500～900 kilograms/meter
3, use temperature: normal temperature～400 ℃.
4, according to the processing method of described coke(oven)gas pre-treatment of claim 1 and partial oxidation preparation of synthetic raw gas, it is characterized in that, the DJ-1 type catalyzer deoxidation that described coke(oven)gas deoxidation pre-treatment selects for use Hubei Province's chemistry to be produced, DJ-1 dehydrogenation catalyst major ingredient: Al
2O
3, portions additive, 3～6 millimeters of granularity φ, bulk density: 700～800 kilograms/meter
3, 100～400 ℃ of use temperatures.
According to the processing method of described coke(oven)gas pre-treatment of claim 1 and partial oxidation preparation of synthetic raw gas, it is characterized in that 5, the low-temperature rectisol desulfurization is adopted in described coke oven gas desulfurization pre-treatment.
6, according to the processing method of described coke(oven)gas pre-treatment of claim 1 and partial oxidation preparation of synthetic raw gas, it is characterized in that, the conversion catalyst that described coke(oven)gas adopts through pretreated coke(oven)gas partial oxidation and steam reforming is the Z204/Z205/CN-20 catalyzer, 450 ℃ of this catalyzer initial activity temperature, anti-1600 ℃ of top temperature; Wherein Z204 is that southwestern chemical research institute produces product, and conversion catalyst is shaped as φ 19 * 19 * 9 mm rounds, major ingredient quality %:NiO 〉=14%, K
2O+Na
2O≤0.2%, Fe
2O
3≤ 0.2%, CaO ≈ 10%, SiO
2≤ 0.2%, Al
2O
3≈ 55%, S≤0.01%, and bulk density: 1160～1190 kilograms/meter 3,450～1350 ℃ of use temperatures; Z205 is that southwestern chemical research institute produces product, and conversion catalyst is shaped as 10 millimeters ring-types of φ 25 * 17 * φ, major ingredient quality %:NiO6 ± 1%, K
2O+Na
2O≤0.2%, Fe
2O
3≈ 0.1%, CaO ≈ 3.5%, SiO
20.2%, Al
2O
3≈ 90%, bulk density: 1100～1150 kilograms/meter
3, use temperature＜1500 ℃; CN-20 is that southwestern chemical research institute produces product, and conversion catalyst is shaped as φ 19 * 9 * 19 ring-types, major ingredient quality %:NaO 〉=14%, K
2O+Na
2O＜0.2%, Fe
2O
3≤ 0.2%, CaO 6%, SiO
2≤ 0.2%, Al
2O
3≈ 76%, bulk density: 0.80 ± 0.05 kilogram/liter, and use temperature＜1200 ℃.
According to the processing method of described coke(oven)gas pre-treatment of claim 1 and partial oxidation preparation of synthetic raw gas, it is characterized in that 7, coke(oven)gas conversion reaction steam/hydrocarbons ratio is not less than 2, carbon ratio 0.6～1.0.
According to the processing method of described coke(oven)gas pre-treatment of claim 1 and partial oxidation preparation of synthetic raw gas, it is characterized in that 8, coke(oven)gas conversion reaction steam/hydrocarbons ratio is not less than 2, carbon ratio 0.7 ± 0.02.
9, the used converter (9) of the processing method of described coke(oven)gas pre-treatment of claim 1 and partial oxidation preparation of synthetic raw gas, it is characterized in that, its converter (9) is an internal heat type partial oxidation furnace structural shape, the inner lining of furnace refractory materials, water jacket is established in the outside, in dress conversion catalyst (14), burner is equipped with the burner mixing burner (20) that oxygenant and coke(oven)gas mixed firing are used; When the oxygenant of oxidation used pure oxygen, burner mixing burner (20) was Switzerland's card Surrey formula burner; When the oxygenant of oxidation used oxygen-rich air, burner mixing burner (20) was built-in multi-hole type burner; Coke(oven)gas and mixture of steam import (16) have been located near burner mixing burner (20) in converter top, and synthetic raw gas outlet (15) is arranged at the converter bottom; Burner mixing burner (20) is provided with entrance of cooling water (17), cooling water outlet (18), and oxidant inlet (19).
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| CN102381717A (en) * | 2010-09-01 | 2012-03-21 | 中国石油天然气股份有限公司 | Method for converting natural gas to produce ammonia and device |
| CN102634369A (en) * | 2012-04-17 | 2012-08-15 | 焦云 | High-temperature coal tar hydrogenation, post-delayed coking and methanol preparation by utilizing coke oven gas combined technology |
| CN103058139A (en) * | 2012-12-31 | 2013-04-24 | 营口三征有机化工股份有限公司 | Method for reproducing medium pressure steam by flare gas generated in synthesis ammonia production process |
| CN106241736A (en) * | 2016-08-03 | 2016-12-21 | 西南化工研究设计院有限公司 | A kind of technique utilizing coke-stove gas extraction metallurgy reducing gases |
| CN110500904A (en) * | 2019-09-20 | 2019-11-26 | 南京聚拓化工科技有限公司 | Integral type ammonia synthesis heat recovery equipment and ammonia synthesis heat recovering process |
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|---|---|---|---|---|
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| CN1680190A (en) * | 2004-04-07 | 2005-10-12 | 庞玉学 | Preparation of methanol synthetic gas from coke oven gas as raw material |
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