CN106350095B - A method of shortening Fischer-Tropsch synthesis system and drives the time - Google Patents
A method of shortening Fischer-Tropsch synthesis system and drives the time Download PDFInfo
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- CN106350095B CN106350095B CN201610721606.3A CN201610721606A CN106350095B CN 106350095 B CN106350095 B CN 106350095B CN 201610721606 A CN201610721606 A CN 201610721606A CN 106350095 B CN106350095 B CN 106350095B
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- synthesis
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
- C10G2/342—Apparatus, reactors with moving solid catalysts
- C10G2/344—Apparatus, reactors with moving solid catalysts according to the "fluidised-bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4031—Start up or shut down operations
Abstract
The present invention relates to the methods of shortening Fischer-Tropsch synthesis system driving time a kind of, gasification crude synthesis gas send to purification and is heated by entering unstripped gas heater after feed gas separator separation condensate, again to pre-transform furnace ash disposal, gaseous mixture out fully enters change furnace reaction, control synthesis gas hydrogen content reaches 80% or more, enters back into low-temp methanol and washes workshop section removing H2S and CO2Purification pneumatic transmission afterwards to synthesis enters synthesis paste state bed reactor, the purified gas come out at the top of synthesis paste state bed reactor enters suction port of compressor surge tank, most of purified gas is vented herein, few a part of purified gas by after synthesis main recycle compressor pressurization with purification come purified gas together with enter reactor, carry out displacement driving.Present invention process need to be replaced through PSA hydrogen manufacturing again, save time swap and conversion gas.
Description
Technical field
The invention belongs to F- T synthesis fields, and in particular to a kind of side for shortening the Fischer-Tropsch synthesis system driving time
Method.
Background technique
Fischer-tropsch synthesis process uses the Fe-series catalyst of Zhong Ke synthetic oil Co., Ltd independent research, system after shutdown of short term
Inflated with nitrogen pressure maintaining requires system hydrogen content that must reach 80% or more, to prevent catalyst coking in reactor when driving
Reduce its reactivity.In the prior art, thick synthesis is produced under halfload using a gasification furnace when shutdown of short term is driven again
Gas about 36000Nm3/ h, wherein H2For content 37% or so, the purified change furnace of crude synthesis gas, which carries out Partial Transformation reaction, becomes hydrogen
Gas content reaches 60% or so conversion gas, unstripped gas of purified gas of the conversion gas after sour gas removes as PSA hydrogen manufacturing, system
Obtain about 9000Nm3The pure hydrogen of/h is replaced into synthesis system, draw again after system displacement is qualified purified gas as synthesis material into
Gas.
It is to send out the normal output of qualified purified gas supply PSA, PSA driving in clean unit to close in previous startup procedure
Synthesis unit, which is sent to, through the pressurization of hydrogenation unit make-up hydrogen compressor after lattice hydrogen carries out system displacement.Due to PSA drive from initially to
Stablize and need certain time and the less limitation of hydrogen producing amount, so synthesis system replacement process when shutdown of short term is driven again every time
At least need 3 hours.
When shutdown of short term is driven again, clean unit output qualification synthetic raw gas supplies PSA (hydrogen manufacturing amount about 9000Nm3/
H), pure hydrogen displacement is carried out into synthesis system, system draws unstripped gas driving again after displacement is qualified；When increasing PSA driving in this way
Between and synthesis system time swap.
Summary of the invention
Goal of the invention of the invention is exactly to shorten synthesis to drive the time, reduces energy consumption.
The present invention is that gasification unit is come to crude synthesis gas to carry out total transform, makes synthesis gas hydrogen content up to 80% or more, passes through
Low-temp methanol wash away except sent after sour gas to synthesis unit carry out system displacement, the short time, that is, replaceable qualification.Not only save
Time swap also reduces a large amount of synthesis gas emptying.
The present invention specifically provides following technical solution：
A method of shortening Fischer-Tropsch synthesis system and drive the time, which is characterized in that gasification crude synthesis gas is sent to net
Change to separate by feed gas separator V1401 and enter unstripped gas heater E1401 after condensate and heat, then to pre-transform furnace ash disposal,
Gaseous mixture out fully enters change furnace R1402 reaction, and control synthesis gas hydrogen content reaches 80% or more, enters back into low temperature
Methanol washes workshop section removing H2S and CO2Purification pneumatic transmission afterwards to synthesis enters synthesis paste state bed reactor R6101, from synthesis slurry bed system
The purified gas come out at the top of reactor R6101 enters suction port of compressor surge tank, and most of purified gas is vented (specific emptying herein
Tolerance prevents catalyst in reactor sedimentation blocking distributor, synthesis reactor air inflow according to the tolerance decision into reactor
100000Nm must not be lower than3/ h), few a part of purified gas by after synthesis main recycle compressor pressurization with purification come purified gas
Enter reactor together, carries out displacement driving, no longer need to replace through PSA hydrogen manufacturing, save time swap and conversion gas.
The present invention has the following advantages that：
1, purification Partial Transformation is changed to total transform, drives to provide necessary condition for synthesis.
2, shorten the time of driving, original technique needs out PSA and hydrogenation compressor before driving, and total transform technique synthesis gas is straight
Synthesis is picked, shorten to half an hour within driving the time 3 hours or more.
3, narrow-minded, displacement is replaced slowly with high-purity hydrogen, PSA is saved in total transform plus hydrogen is driven the time, is reduced synthesis and is set
Change the time；
4, total transform driving unstripped gas is not vented, and is reduced consumption, is reduced Environmental costs；It increases economic efficiency.
Detailed description of the invention
Fig. 1 is present invention process flow diagram
Wherein,V1401Feed gas separator,R1401A/BPre-transform furnace,E1401Raw material hot-air heater,R1402Transformation
Furnace,R6101Fischer-Tropsch synthesis device,K7102Make-up hydrogen compressor,K6101Main recycle compressor；
Specific embodiment
Under nominal situation, the crude synthesis gas come that gasifies crosses transformation by HV1424 and HV1424N regulating valve adjustment portion lease making
Furnace makes to convert outlet of still content H2Reach 65% or so, then washes workshop section removing H through low-temp methanol2S and CO2Part purified gas is sent afterwards
PSA hydrogen manufacturing, part are vented, and PSA generates H2After be sent to plus hydrogen, add hydrogen starting make-up hydrogen compressor sending synthesis unit after pressurized with hydrogen
Displacement, not only wastes Partial Transformation gas and time in this way, and since R1402 is narrow-minded when Partial Transformation is driven, reaction heat
Band is not walked, it is easy to change furnace R1402 temperature runaway (this driving before ninety-nine times out of a hundred all temperature runaway) occur；It is excellent by technique at this stage
After change, gasification crude synthesis gas is sent condensate is separated by feed gas separator V1401 to purification after enter E1401 and heat, then to pre-
Change furnace ash disposal, gaseous mixture out make crude synthesis gas fully enter R1402 transformation by closing HV1424 and HV1424N valve position entirely
Furnace reaction, control synthesis gas hydrogen content reach 80% or more, enter back into low-temp methanol and wash workshop section removing H2S and CO2Purification afterwards
Pneumatic transmission to synthesis enters synthesis paste state bed reactor R6101, and the purified gas come out from the top R6101 enters suction port of compressor and buffers
Tank, most of purified gas is vented herein (to be specifically vented tolerance according to the tolerance decision into reactor, prevents catalyst in reactor
Sedimentation blocking distributor, synthesis reactor air inflow must not be lower than 100000Nm3/ h), few a part of purified gas passes through synthesis master
Enter reactor together with the purified gas that purification comes after recycle compressor K6101 pressurization, carries out displacement driving, no longer need to through PSA
Hydrogen manufacturing displacement, saves time swap and conversion gas.
This patent can be realized using ready-made process, not need change process.Gasification crude synthesis gas, which is sent to purification, to be passed through
V1401, which is separated, to be entered E1401 after condensate and heats, then to pre-transform furnace ash disposal, gaseous mixture out by close full HV1424 and
HV1424N valve position makes crude synthesis gas fully enter the reaction of R1402 change furnace, and control synthesis gas hydrogen content reaches 80% or more,
It enters back into low-temp methanol and washes workshop section removing H2S and CO2Purification pneumatic transmission afterwards to synthesize into synthesis paste state bed reactor R6101, from
The purified gas come out at the top of R6101 enters suction port of compressor surge tank, and most of purified gas is vented (specific emptying tolerance root herein
According into reactor tolerance and system pressure determine, prevent catalyst in reactor sedimentation blocking distributor, synthesis reactor into
Tolerance must not be lower than 100000Nm3/ h), few a part of purified gas by after synthesis main recycle compressor K6101 pressurization with purification
The purified gas come enters reactor together, carries out displacement driving
Term is explained：
F- T synthesis (also known as F-T synthesis)：One of ICL for Indirect Coal Liquefaction technology is raw material in catalyst (this list using synthesis gas
Position is Fe-series catalyst) and appropriate reaction under the conditions of synthesize the technical process of liquid fuel based on paraffin hydrocarbon.
CO shift reaction (referred to as converts)：Under certain condition, the carbon monoxide and vapor in semiwater gas are anti-
The technical process of hydrogen and carbon dioxide should be generated.
Claims (1)
1. a kind of method for shortening the Fischer-Tropsch synthesis system driving time, which is characterized in that gasification crude synthesis gas is sent to purification
It is separated by feed gas separator and enters unstripped gas heater after condensate and heat, then to pre-transform furnace ash disposal, gaseous mixture out
Change furnace reaction is fully entered, control synthesis gas hydrogen content reaches 80% or more, enters back into low-temp methanol and washes workshop section removing H2S
And CO2Purification pneumatic transmission afterwards to synthesis enters synthesis paste state bed reactor, the purification come out at the top of synthesis paste state bed reactor
Gas enters suction port of compressor surge tank, and most of purified gas is vented herein, and few a part of purified gas passes through synthesis major cycle compression
Enter reactor together with the purified gas that purification comes after machine pressurization, carry out displacement driving, no longer need to replace through PSA hydrogen manufacturing, saves
Time swap and conversion gas；Specific emptying tolerance prevents catalyst in reactor from settling according to the tolerance decision into reactor
Distributor is blocked, synthesis reactor air inflow must not be lower than 100000Nm3/h。
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| CN106350095B true CN106350095B (en) | 2018-11-30 |
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| CN108285809B (en) * | 2018-01-08 | 2020-02-21 | 内蒙古伊泰煤基新材料研究院有限公司 | Start-up method of double series Fischer-Tropsch reaction device |
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| US4626552A (en) * | 1986-01-06 | 1986-12-02 | Exxon Research And Engineering Company | Process for the start-up of a Fischer-Tropsch reactor |
| WO2007069197A2 (en) * | 2005-12-15 | 2007-06-21 | Sasol Technology (Proprietary) Limited | Production of hydrocarbons from natural gas |
| US9464237B2 (en) * | 2012-09-05 | 2016-10-11 | Haldor Topsoe A/S | Method for starting-up a gas to liquid process |
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| CN104176705B (en) * | 2014-08-08 | 2016-05-25 | 山东齐鲁科力化工研究院有限公司 | A kind of sulfur resistant conversion process of producing synthesis gas |
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