CN101381616A - Technique for producing oil products by fischer-tropsch synthesis - Google Patents
Technique for producing oil products by fischer-tropsch synthesis Download PDFInfo
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Abstract
The invention relates to a technological method for preparing oil products by the Fischer-Tropsch synthesis. In the technological method, a FT synthesis process comprises a first-stage FT synthesis process and a second-stage FT synthesis process; in particular, the technological method comprises the following steps: (1) synthesis gases are subjected to FT synthesis reaction in a first-stage synthesis reactor; (2) a part of tail gases from the first-stage synthesis reactor are circularly returned to an entrance of the first-stage synthesis reactor, and another part of the tail gases enter a second-stage synthesis reactor for the further FT synthesis reaction; (3) a part of tail gases from the second-stage synthesis reactor are circularly returned to an entrance of the second-stage synthesis reactor, and another part of the tail gases are used for reclaiming low-carbon hydrocarbons and hydrogen gases and then are used as fuel gases; and (4) by utilizing the recovered hydrogen gases, the hydrocarbon products in the first-stage synthesis reactor and the second-stage synthesis reactor and the hydrocarbon products which are obtained by separating and recovering the tail gases are subjected to hydrogenation and purification and then are fractionated to generate various oil products. Compared with prior art, the technological method has the characteristics of economy, flexibility, low cost and the like.
Description
Technical field
The present invention relates to the oil manufacture method, relating in particular to a kind of is that raw material adopts the synthetic processing method of producing liquid oil of Fischer-Tropsch with the synthetic gas.
Background technology
With coal or Sweet natural gas is that raw material is produced synthetic gas, synthetic gas is by the Fischer-Tropsch synthesis synthin, one step of hydro carbons is processed as the ICL for Indirect Coal Liquefaction process of liquid oil, is one of important technology developing direction of 21st century clean energy utilization and energy substitution strategy.
According to the main result of existing Literature Consult, the Fischer-Tropsch building-up process is summarized as follows:
Synthetic gas is with H
2With CO be main mixed gas, Fischer-Tropsch synthesis takes place under the effect of fischer-tropsch synthetic catalyst generate the liquid hydrocarbon product.Depend on reactor pattern, processing condition, catalyst type etc. by synthetic product kind and the quantity that obtains of Fischer-Tropsch.Fischer-Tropsch building-up process catalyzer commonly used is cobalt-base catalyst and ferrum-based catalyst, can be divided into high temperature and low temperature Fischer-Tropsch building-up process by the reactor service temperature, that reactor types mainly contains is tubular fixed-bed, four kinds of circulating fluidized beds, fixed fluidized bed and slurry attitude bed etc.Go out the general containing water vapor of logistics, carbonic acid gas, the unreacted synthesis gas (H of Fischer-Tropsch synthesis device
2And CO), carburet hydrogen (C1-C4), liquid hydrocarbon (C5+), oxygenatedchemicals and N
2Deng.Through condensation with separate, can obtain several streams of liquid hydrocarbon, reaction water and reaction end gas strand.The product upgrading workshop section of liquid hydrocarbon in the downstream processed obtains processed oil.
In the prior art, the Fischer-Tropsch building-up process adopts the single-stage Fischer-Tropsch synthetic usually, unreacted synthesis tail gas partly loops back synthesis reactor to improve the oil product productive rate of unit synthetic gas, and all the other tail gas are made fuel gas through further reclaiming wherein after useful component such as lower carbon number hydrocarbons and the hydrogen etc.The main drawback of this method is: at same material gas quantity with under forming, because the composition of synthesis tail gas and unstripped gas differs greatly, enter the H of reactor on the one hand
2Ideal value of the difficult assurance of/CO, the oil product space-time yield is lower; The increase of recycle ratio must mean the increase into synthesis reactor tolerance on the other hand, if do not change the operating linear velocity of single reactor, the single reactor required diameter that reaches with equal yield line significantly increases, otherwise number of reactors increases, and has strengthened the size of reactor and gas tube and has increased manufacture difficulty and cost; In addition, because a large amount of gas circulation is returned reactor inlet, consumption of compressor is also bigger.
In view of this, a two-stage Fischer-Tropsch synthetic notion has been proposed among the patent ZL200310108146.X (a kind of processing method with the synthesis gas producing fluid fluid fuel), be that the Fischer-Tropsch synthesis device is divided into two-stage, the circulation of an one-level Fischer-Tropsch synthetic tail gas part guarantees comparatively ideal reactor inlet H
2/ CO ratio, a part enters the reaction of secondary Fischer-Tropsch synthesis device in addition, the tail gas part circulation of secondary Fischer-Tropsch synthesis, a part goes follow-up C3-C5 to reclaim the unit.
The advantage of this patent proposition method is: by adjusting two-stage Fischer-Tropsch synthetic recycle ratio, can guarantee higher synthetic oil product productive rate; Simultaneously, because one-level tail gas need not boost and can enter secondary Fischer-Tropsch synthesis device, and in synthetic oil product afterreaction contraction of gas, the recycle gas flow greatly reduces, power consumption is lower, and the reactor diameter of secondary synthesis reactor, gas delivery pipeline are also less like this.
But the secondary Fischer-Tropsch synthetic technology that this patent proposes has the following disadvantages:
(1) this technology can not dispose the reactor pattern that is applicable to different Fischer-Tropsch building-up processes according to product demand only at low temperature Fischer-Tropsch building-up process.
(2) corresponding relation of not clear and definite one-level and secondary synthesis reactor in the disclosed scheme of this technology, according to embodiment, implicit scheme is that each one-level synthesis reactor is corresponding to a secondary synthesis reactor, because secondary synthesis reactor inlet tolerance is significantly less than the one-level synthesis reactor, so secondary synthesis reactor size is also far below the one-level synthesis reactor, the processing power of the single reactor of one-level secondary differs greatly.
(3) one-level tail gas promptly loops back A reactor and enters second reactor without any processing in the disclosed scheme of this technology, and secondary tail gas promptly loops back second reactor without any processing, and other component in the gas (mainly is CO
2) except that the reaction dividing potential drop that reduces effective gas, increase gas flow also will increase the reactor design diameter, the circulation power consumption also can increase.
Summary of the invention
Purpose of the present invention is exactly the processing method that a kind of economy, the oil product of the synthetic production of Fischer-Tropsch flexibly are provided for the defective that overcomes above-mentioned prior art existence.
Purpose of the present invention can be achieved through the following technical solutions:
The synthetic processing method of producing oil product of a kind of Fischer-Tropsch is characterized in that the Fischer-Tropsch building-up process that this method adopts comprises placed in-line one-level Fischer-Tropsch building-up process and secondary Fischer-Tropsch building-up process, specifically may further comprise the steps:
(1) Fischer-Tropsch synthesis takes place in synthetic gas in the one-level synthesis reactor, and the reactor outlet product is separated into liquid hydro-carbon products, contains the reaction water and the tail gas of organic oxygenatedchemicals;
(2) the tail gas part of one-level synthesis reactor loops back one-level synthesis reactor inlet, another part enters the secondary synthesis reactor Fischer-Tropsch synthesis further takes place, and secondary synthesis reactor outlet product is separated into liquid hydro-carbon products, contains the reaction water and the tail gas of organic oxygenatedchemicals;
(3) the tail gas part of secondary synthesis reactor loops back secondary synthesis reactor inlet, and another part is used as fuel gas after reclaiming lower carbon number hydrocarbons, hydrogen;
(4) hydrogen that utilize to reclaim is to producing multiple oil product after the hydrocarbon product hydrogenation upgrading of Separation and Recovery in one-level synthesis reactor, secondary synthesis reactor and the tail gas and the fractionation.
Described one-level Fischer-Tropsch building-up process and secondary Fischer-Tropsch building-up process can be according to the requirement of target product being adopted the synthetic or high temperature fischer-tropsch building-up process of low temperature Fischer-Tropsch.
Described one-level synthesis reactor can adopt different reactor patterns according to the requirement to target product with the secondary synthesis reactor.
Described different reactor pattern comprises fixed-bed reactor, paste state bed reactor and fluidized-bed reactor.
Described one-level synthesis reactor is one or more reactor parallel connection, and described secondary synthesis reactor is one or more reactor parallel connection.
When described A reactor number was a plurality of, the equipment size of single secondary synthesis reactor was approaching or consistent with single one-level synthesis reactor.
The tail gas of the tail gas of described one-level synthesis reactor, secondary synthesis reactor is all or part of to be entered one and removes non-effective gas unit, and non-effective qi exhaustion is removed, and improves to enter one-level, secondary synthesis reactor again after effective pneumatolytic divides.
Described effective gas is H
2, the CO gaseous fraction, non-effective gas is H
2, the remaining gas component beyond the CO.
Described non-effective gas unit that removes is for removing CO
2The unit.
Compared with prior art, the present invention has following characteristics:
(1) adopt the two-stage Fischer-Tropsch synthetic, the one-level synthesis reactor can adopt different reactor patterns with the secondary synthesis reactor, and products scheme is more flexible like this.
(2) handle number and the size that tolerance disposes reactor according to secondary Fischer-Tropsch synthetic, can realize that one-level secondary synthesis reactor size is approaching or consistent, reduce number of reactors, reduced the manufacturing cost of reactor and relevant device, subsidiary pipeline.
(3) one-level, secondary Fischer-Tropsch process exhaust enter reactor after all can removing non-effective gas earlier again, have improved the effective pneumatolytic branch of reactor inlet, can improve the space-time yield of oil product; Compare with hydro carbons method in the steam reforming tail gas of part bibliographical information, saved the investment cost and the operation energy consumption of steam reforming stove, and effectively the above carburet hydrogen of C2 in the gas can not transform simultaneously with the conversion of CH4, can not cause the loss of hydrocarbon.
Description of drawings
Fig. 1 is a kind of two-stage Fischer-Tropsch synthesis process flow process of form;
Fig. 2 is the two-stage Fischer-Tropsch synthesis process flow process of another form;
Fig. 3 is the two-stage Fischer-Tropsch synthesis process flow process of another form.
Embodiment
Embodiment will reach the following examples illustrated in conjunction with the accompanying drawings.
The present embodiment principal feature is, adopts the two-stage Fischer-Tropsch synthetic, and wherein one-level Fischer-Tropsch synthesis device is two parallel connections, and secondary Fischer-Tropsch synthesis device is a separate unit.As shown in Figure 1, wherein one-level Fischer-Tropsch synthesis device is two parallel reactors, and secondary Fischer-Tropsch synthesis device is single.One-level, the synthetic low temperature Fischer-Tropsch that is of secondary Fischer-Tropsch synthesize, and adopt paste state bed reactor.
The overhead gas stream thigh 16 of one-level quenching column 11 and one-level quenching column 21 and overhead gas stream thigh 26 are merged into gas streams 29, earlier after after two- stage cooler 30 and 31 was cooled to 40 ℃, enter high-pressure separator 32 and separate: oil phase hydrocarbons 33 was as cryogenic condensation produce product; Water product 34 is for being rich in the reaction water of oxygenatedchemicals; Gas phase is an one-level synthesis tail gas 35.
One-level synthesis tail gas 35 is 720000Nm
3/ h is divided into two strands: the flow of stream thigh 36 is 440000Nm
3/ h returns one-level synthesis reactor inlet after compressed machine 37 compressions; Stream thigh 38 is 280000Nm
3/ h sends to secondary Fischer-Tropsch synthesis system.
Secondary synthesis tail gas 57 is 359000Nm
3/ h is divided into two strands: the flow of stream thigh 58 is 239000Nm
3/ h returns secondary synthesis reactor inlet after compressed machine 59 compressions; Stream thigh 60 is 120000Nm
3/ h goes to make fuel gas behind follow-up system recovery lower carbon number hydrocarbons, the hydrogen.
In the present embodiment, single one-level Fischer-Tropsch synthesis device is identical with the diameter of secondary Fischer-Tropsch synthesis device, is 6.33m.Each one-level Fischer-Tropsch synthesis device catalyzer loading amount is 128.35t, and secondary Fischer-Tropsch synthesis device catalyzer loading amount is 118.45t, and the catalyzer inventory is 375.15t.
In the present embodiment, one-level Fischer-Tropsch synthin product volume is: paraffin 57.00t/h, high temperature condensation product 17.64t/h, cryogenic condensation thing 17.32t/h; Secondary Fischer-Tropsch synthin product volume is: paraffin 12.30t/h, high temperature condensation product 7.49t/h, cryogenic condensation thing 11.77t/h.Recyclable lower carbon number hydrocarbons product 12.85t/h (comprising LPG cut and C5+ cut) from the secondary Fischer-Tropsch process exhaust, then total hydrocarbon products amount is 136.37t/h, the corresponding about 364g/kg.cat.h of oil product space-time yield, CO+CO
2Total conversion rate 79.50%.
Under the operational condition of present embodiment, one-level synthesis reactor inlet H
2/ CO ratio is 1.71, secondary synthesis reactor inlet H
2/ CO ratio is 1.95, calculates according to the rate of recovery of the required hydrogen of oil hydrogenation upgrading and 90%, and stream strand 60 need 70% enter recovery hydrogen unit and can satisfy the demand, and maybe can reduce and reclaim the unitary design organic efficiency of hydrogen.The oil from Fischer-Tropsch synthesis of this embodiment (lower carbon number hydrocarbons that comprises recovery) will mainly obtain diesel oil, petroleum naphtha and LPG oil product after hydrogenation upgrading, fractionation, ultimate production is 1,080,000 tons/year (operating 8000 hours meters per year).
If secondary Fischer-Tropsch synthesis unit also adopts two synthesis reactor parallel connections, though then increased the handiness of operation, but table of equipment number and pipeline all increase, and it is less (if keep equal operating linear velocity that the second reactor size is compared with one-level synthesis reactor size, reactor size will be reduced to 4.48m), be unfavorable for the seriation of making, manufacturing cost increases.
The pressure of fresh synthesis gas, flow and gas composition are identical with embodiment 1.
One- level quenching column 71 and 81 overhead gas stream strands 76 and 86 is merged into gas streams 89, earlier after after two- stage cooler 90 and 91 was cooled to 40 ℃, enter high-pressure separator 92 and separate: oil phase hydrocarbons 93 was as cryogenic condensation produce product; Water product 94 is for being rich in the reaction water of oxygenatedchemicals; Gas phase is an one-level synthesis tail gas 95.
One-level synthesis tail gas 95 is 720000Nm
3/ h is divided into two strands: the flow of stream thigh 96 is 440000Nm
3/ h returns one-level synthesis reactor inlet after compressed machine 97 compressions; Stream thigh 98 is 280000Nm
3/ h sends to secondary Fischer-Tropsch synthesis system.
Secondary synthesis tail gas 117 is 341000Nm
3/ h is divided into two strands: the flow of stream thigh 118 is 274000Nm
3/ h enters the decarburization unit and removes wherein CO
2After, flow is kept to 239000Nm3/h, CO
2Content reduces to 0.01% by 13.02%, returns secondary synthesis reactor inlet after compressed again machine 120 compressions; Stream thigh 121 is 67000Nm
3/ h goes to make fuel gas behind follow-up system recovery lower carbon number hydrocarbons, the hydrogen.
In the present embodiment, because reactor size is identical with embodiment 1, so the catalyzer loading amount is also identical, the catalyzer inventory is 375.15t.
In the present embodiment, one-level Fischer-Tropsch synthin product volume is all mutually with embodiment 1: paraffin 57.00t/h, high temperature condensation product 17.64t/h, cryogenic condensation thing 17.32t/h; Secondary Fischer-Tropsch synthin product volume is different with embodiment 1, for: paraffin 14.13t/h, high temperature condensation product 8.18t/h, cryogenic condensation thing 13.88t/h.Recyclable lower carbon number hydrocarbons product 11.00t/h (comprising LPG cut and C5+ cut) from the secondary Fischer-Tropsch process exhaust, then total hydrocarbon products amount is 139.15t/h, the corresponding about 371g/kg.cat.h of oil product space-time yield, CO+CO
2Total conversion rate 81.11%. increases than embodiment 1.As seen constant (linear speed is constant at reactor size, mean that promptly recycle ratio is constant, go downstream section tail gas amount to reduce) situation under, the recirculation bout becomes reactor after the tail gas decarburization, though equipment size such as compression power consumption and reactor, compressor changes little, help improving the productive rate of oil product.
Under the operational condition of present embodiment, one-level synthesis reactor inlet H
2/ CO ratio is 1.71, secondary synthesis reactor inlet H
2/ CO ratio is 2.10, calculates according to the rate of recovery of the required hydrogen of oil hydrogenation upgrading and 90%, and stream thigh 121 need all enter recovery hydrogen unit and just can satisfy the demand.This explanation though embodiment 2 increases than embodiment 1 oil product output, has increased a decarburization unit (or having increased the unitary treatment capacity of follow-up decarburization), and equipment and process cost increase, and reclaiming unitary organic efficiency of hydrogen or processing power simultaneously will increase.
The oil from Fischer-Tropsch synthesis (lower carbon number hydrocarbons that comprises recovery) that this embodiment obtains will mainly obtain diesel oil, petroleum naphtha and LPG oil product after hydrogenation upgrading, fractionation, ultimate production is 1,100,000 tons/year (operating 8000 hours meters per year).
The pressure of fresh synthesis gas, flow and gas composition are identical with embodiment 1.
Fresh synthesis gas 122 is mixed into gas streams 124 with one-level synthesis cycle tail gas 123 and is equally divided into two plume thighs 126 and 137 after interchanger 125 preheating, enter the reaction-Quench unit of flow setting and identical two parallel connections of equipment installation size: stream strands 126 in interchanger 127 with tower still stream burst 133 heat exchange from quenching column 129, be heated to and enter one-level synthetic pulp state bed reactor 129 about 140 ℃, stream strands 137 in interchanger 138 with tower still stream burst 143 heat exchange from quenching column 139, be heated to and enter one-level synthetic pulp state bed reactor 139 about 140 ℃, under the effect of low temperature fischer-tropsch catalysts, 2.8MPaG, 240 ℃ Fischer-Tropsch synthesis takes place down, generate Fischer-Tropsch synthetic: liquid product 130 and liquid product 140 paraffin are as the product extraction, gas-phase product 131 enters the 132 cooling washings of one-level quenching column, and gas-phase product 141 enters the 142 cooling washings of one-level quenching column.Part liquid phase discharging 135 extraction of one-level quenching column 132 bottoms are high temperature condensation product product, and part liquid phase discharging 145 extraction of one-level quenching column 142 bottoms are high temperature condensation product product; 134 circulations of a part of in addition liquid phase discharging 133 usefulness recycle pumps, be cooled to 110 ℃ through interchanger 127, interchanger 128 and enter one-level quenching column 132 cats head, making tower top outlet gas 136 temperature is 130 ℃, 144 circulations of a part of in addition liquid phase discharging 143 usefulness recycle pumps, be cooled to 110 ℃ through interchanger 138, interchanger 146 and enter one-level quenching column 142 cats head, making tower top outlet gas 147 temperature is 130 ℃.Stream thigh 130 and stream thigh 140 are merged into one-level paraffinic product stream thigh 148, and stream thigh 135 and stream thigh 145 are merged into one-level high temperature condensation product product flow thigh 149.
One- level quenching column 132 and 142 overhead gas stream strands 136 and 147 is merged into gas streams 150, earlier after after two- stage cooler 151 and 152 was cooled to 40 ℃, enter high-pressure separator 153 and separate: oil phase hydrocarbons 154 was as cryogenic condensation produce product; Water product 155 is for being rich in the reaction water of oxygenatedchemicals; Gas phase is an one-level synthesis tail gas 156.
One-level synthesis tail gas 156 is 720000Nm
3/ h is divided into two strands: the flow of stream thigh 157 is 440000Nm
3/ h returns one-level synthesis reactor inlet after compressed machine 158 compressions; Stream thigh 159 is 280000Nm
3/ h sends to secondary Fischer-Tropsch synthesis system.
Gas streams 159 from one-level Fischer-Tropsch synthesis system is mixed with secondary synthesis cycle tail gas 161, mix back gas streams 160 through interchanger 162,163 two-stage heat exchange, be heated to about 140 ℃, enter secondary resultant current fluidized bed reactor 164, under the effect of high temperature fischer-tropsch catalyzer, 2.4MPaG 350 ℃ Fischer-Tropsch synthesis takes place down, gaseous phase outlet product 165 enters the 166 cooling washings of secondary quenching column.Part liquid phase discharging 167 extraction of secondary quenching column 166 bottoms are secondary high temperature condensation product product; 169 circulations of a part of in addition liquid phase discharging 168 usefulness recycle pumps are cooled to 130 ℃ through interchanger 163, interchanger 170 and enter secondary quenching column 166 cats head, and making tower top outlet gas 171 temperature is 190 ℃.Tower top outlet gas 171 is earlier after after two- stage cooler 172 and 173 was cooled to 40 ℃, enter high-pressure separator 174 and separate: oil phase hydrocarbons 175 was as cryogenic condensation produce product; Water product 176 is for being rich in the reaction water of oxygenatedchemicals; Gas phase is a secondary synthesis tail gas 177.
Secondary synthesis tail gas 177 is 375000Nm
3/ h is divided into two strands: the flow of stream thigh 178 is 274000Nm
3/ h enters the decarburization unit and removes wherein CO
2After, flow is kept to 239000Nm3/h, CO
2Content reduces to 0.01% by 13.02%, returns secondary synthesis reactor inlet after compressed again machine 180 compressions; Stream thigh 181 is 53000Nm
3/ h goes to make fuel gas behind follow-up system recovery lower carbon number hydrocarbons, the hydrogen.
In the present embodiment, reactor size is identical with embodiment 1, so the catalyzer loading amount is also identical, the catalyzer inventory is 375.15t.
In the present embodiment, one-level Fischer-Tropsch synthin product volume is identical with embodiment 1,2, for: paraffin 57.00t/h, high temperature condensation product 17.64t/h, cryogenic condensation thing 17.32t/h; Secondary Fischer-Tropsch synthin product volume is different with embodiment 1,2, for: high temperature condensation product 2.41t/h, cryogenic condensation thing 31.78t/h.Recyclable lower carbon number hydrocarbons product 12.48t/h from the secondary Fischer-Tropsch process exhaust, then total hydrocarbon products amount is 138.63t/h, the corresponding about 370g/kg.cat.h of oil product space-time yield, CO+CO
2Total conversion rate 83.20%.CO+CO
2Total conversion rate improves than embodiment 2, but the decline of total hydrocarbon productive rate, this is to be higher than last embodiment because a part reclaims the short hydrocarbon amount that enters fuel gas system of not getting off.
Under the operational condition of present embodiment, one-level synthesis reactor inlet H
2/ CO ratio is 1.71, secondary synthesis reactor inlet H
2/ CO ratio is 3.19, calculates according to the required amounts of hydrogen of oil hydrogenation upgrading, and stream strands 121 need all enter and reclaim hydrogen unit and the rate of recovery and reach more than 95% and just can satisfy the demand.This is because high-temperature Fischer-Tropsch synthesis reaction device inlet must keep high H
2The reason of/CO ratio.
One-level oil from Fischer-Tropsch synthesis and secondary oil from Fischer-Tropsch synthesis that this embodiment obtains carry out will mainly obtaining diesel oil, gasoline, petroleum naphtha and LPG and olefin product (operating 8000 hours meters per year) after hydrogenation upgrading, the fractionation, annual production is 1,100,000 tons, product structure is than horn of plenty, added value of product is higher, can realize high economic benefit.
Foregoing has been described the preferred embodiments of the invention; but should be understood to also have many adjustable places; all adopt fluidized-bed reactor etc. as one section tail gas being carried out decarburization, two sections; these concrete selections of improving one's methods are directly related with each factors such as facility investment, process cost and products scheme, but all should be in protection scope of the present invention.
Claims (9)
1. the processing method of the synthetic production of a Fischer-Tropsch oil product is characterized in that, the Fischer-Tropsch building-up process of this method employing comprises placed in-line one-level Fischer-Tropsch building-up process and secondary Fischer-Tropsch building-up process, specifically may further comprise the steps:
(1) Fischer-Tropsch synthesis takes place in synthetic gas in the one-level synthesis reactor, and the reactor outlet product is separated into liquid hydro-carbon products, contains the reaction water and the tail gas of organic oxygenatedchemicals;
(2) the tail gas part of one-level synthesis reactor loops back one-level synthesis reactor inlet, another part enters the secondary synthesis reactor Fischer-Tropsch synthesis further takes place, and secondary synthesis reactor outlet product is separated into liquid hydro-carbon products, contains the reaction water and the tail gas of organic oxygenatedchemicals;
(3) the tail gas part of secondary synthesis reactor loops back secondary synthesis reactor inlet, and another part is used as fuel gas after reclaiming lower carbon number hydrocarbons, hydrogen;
(4) hydrogen that utilize to reclaim is to producing multiple oil product after the hydrocarbon product hydrogenation upgrading of Separation and Recovery in one-level synthesis reactor, secondary synthesis reactor and the tail gas and the fractionation.
2. the synthetic processing method of producing oil product of a kind of Fischer-Tropsch according to claim 1, it is characterized in that described one-level Fischer-Tropsch building-up process and secondary Fischer-Tropsch building-up process can be according to the requirement of target product being adopted the synthetic or high temperature fischer-tropsch building-up process of low temperature Fischer-Tropsch.
3. the synthetic processing method of producing oil product of a kind of Fischer-Tropsch according to claim 1 is characterized in that, described one-level synthesis reactor can adopt different reactor patterns according to the requirement to target product with the secondary synthesis reactor.
4. the synthetic processing method of producing oil product of a kind of Fischer-Tropsch according to claim 3 is characterized in that described different reactor pattern comprises fixed-bed reactor, paste state bed reactor and fluidized-bed reactor.
5. the synthetic processing method of producing oil product of a kind of Fischer-Tropsch according to claim 1 is characterized in that described one-level synthesis reactor is one or more reactor parallel connection, and described secondary synthesis reactor is one or more reactor parallel connection.
6. the synthetic processing method of producing oil product of a kind of Fischer-Tropsch according to claim 5 is characterized in that, when described A reactor number was a plurality of, the equipment size of single secondary synthesis reactor was approaching or consistent with single one-level synthesis reactor.
7. the synthetic processing method of producing oil product of a kind of Fischer-Tropsch according to claim 1, it is characterized in that, the tail gas of the tail gas of described one-level synthesis reactor, secondary synthesis reactor is all or part of to be entered one and removes non-effective gas unit, non-effective qi exhaustion is removed, improve and enter one-level, secondary synthesis reactor again after effective pneumatolytic divides.
8. the synthetic processing method of producing oil product of a kind of two-stage Fischer-Tropsch according to claim 7 is characterized in that described effective gas is H
2, the CO gaseous fraction, non-effective gas is H
2, the remaining gas component beyond the CO.
9. the synthetic processing method of producing oil product of a kind of two-stage Fischer-Tropsch according to claim 7 is characterized in that described non-effective gas unit that removes is for removing CO
2The unit.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101955788A (en) * | 2010-07-09 | 2011-01-26 | 神华集团有限责任公司 | Fischer-Tropsch synthesis method and system |
| CN101863728B (en) * | 2009-04-17 | 2013-06-05 | 中国石油化工股份有限公司 | Fischer-Tropsch synthesis method |
| CN104910960A (en) * | 2015-05-19 | 2015-09-16 | 上海兖矿能源科技研发有限公司 | Method for producing n-alkane solvent oil from Fischer-Tropsch synthetic oil |
| CN111286354A (en) * | 2020-02-29 | 2020-06-16 | 上海兖矿能源科技研发有限公司 | Method and device for producing hydrocarbons by two-stage series connection of low-temperature Fischer-Tropsch and high-temperature Fischer-Tropsch |
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| CN103396826B (en) * | 2013-08-14 | 2015-06-10 | 神华集团有限责任公司 | Two-stage series-connected Fischer-Tropsch synthesis system and process thereof |
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| CN1281714C (en) * | 2003-10-27 | 2006-10-25 | 上海兖矿能源科技研发有限公司 | Liquid fuel producing technique from synthetic gas |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101863728B (en) * | 2009-04-17 | 2013-06-05 | 中国石油化工股份有限公司 | Fischer-Tropsch synthesis method |
| CN101955788A (en) * | 2010-07-09 | 2011-01-26 | 神华集团有限责任公司 | Fischer-Tropsch synthesis method and system |
| WO2012003806A1 (en) * | 2010-07-09 | 2012-01-12 | 神华集团有限责任公司 | A fischer-tropsch synthesis process and system |
| CN101955788B (en) * | 2010-07-09 | 2013-05-22 | 神华集团有限责任公司 | Fischer-Tropsch synthesis method and system |
| RU2562770C2 (en) * | 2010-07-09 | 2015-09-10 | Шэньхуа Груп Корпорэйшн Лимитед | Method and device for carrying out fischer-tropsch synthesis |
| CN104910960A (en) * | 2015-05-19 | 2015-09-16 | 上海兖矿能源科技研发有限公司 | Method for producing n-alkane solvent oil from Fischer-Tropsch synthetic oil |
| CN111286354A (en) * | 2020-02-29 | 2020-06-16 | 上海兖矿能源科技研发有限公司 | Method and device for producing hydrocarbons by two-stage series connection of low-temperature Fischer-Tropsch and high-temperature Fischer-Tropsch |
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