CN107964417A - A kind of method and system of preparing gasoline by methanol - Google Patents
A kind of method and system of preparing gasoline by methanol Download PDFInfo
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- CN107964417A CN107964417A CN201610906036.5A CN201610906036A CN107964417A CN 107964417 A CN107964417 A CN 107964417A CN 201610906036 A CN201610906036 A CN 201610906036A CN 107964417 A CN107964417 A CN 107964417A
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- gasoline
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 221
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000001816 cooling Methods 0.000 claims abstract description 44
- 239000003915 liquefied petroleum gas Substances 0.000 claims abstract description 36
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 24
- 238000009834 vaporization Methods 0.000 claims abstract description 18
- 230000008016 vaporization Effects 0.000 claims abstract description 18
- 230000001351 cycling effect Effects 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 9
- WVDDGKGOMKODPV-UHFFFAOYSA-N Benzyl alcohol Chemical compound OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229960004217 benzyl alcohol Drugs 0.000 claims abstract description 8
- 230000003197 catalytic effect Effects 0.000 claims description 60
- 229930195733 hydrocarbon Natural products 0.000 claims description 31
- 239000004215 Carbon black (E152) Substances 0.000 claims description 30
- 150000002430 hydrocarbons Chemical class 0.000 claims description 30
- 239000000203 mixture Substances 0.000 claims description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 238000010438 heat treatment Methods 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 239000003381 stabilizer Substances 0.000 claims description 15
- 238000013021 overheating Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 8
- 150000001875 compounds Chemical class 0.000 claims description 5
- 239000002808 molecular sieve Substances 0.000 claims description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 3
- 230000005540 biological transmission Effects 0.000 claims description 2
- 239000004575 stone Substances 0.000 claims description 2
- 230000006641 stabilisation Effects 0.000 claims 1
- 238000011105 stabilization Methods 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 abstract 1
- 239000000126 substance Substances 0.000 abstract 1
- 230000008901 benefit Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- -1 methanol hydrocarbon Chemical class 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
Classifications
-
- 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to the process and system of a kind of preparing gasoline by methanol, described method includes following steps：By material benzenemethanol by boosting, preheating, vaporization, overheat, catalysis, cooling, separation and etc., obtain gasoline products, and by the abundant cycling and reutilization of the liquefied petroleum gas of generation, at the same time, the accessory substance circulating air produced in process of production carries out Recycling, and heat exchange loop is devised in systems, improve utilization rate of the system to material and energy.The method and system of the present invention realizes the clean gasoline using methanol high value, meets China market clean gasoline product demand in short supply, improves the economy and commercial value of technique for preparing gasoline by methanol.
Description
Technical field
Exist the present invention relates to the process and system of a kind of preparing gasoline by methanol, more particularly to using methanol and recycled offgas
The method and system of gasoline processed is realized under the action of catalyst, the present invention is suitable for preparing gasoline by methanol, improves preparing gasoline by methanol
Selectivity.
Background technology
At present, as the requirement that the development of Chinese national economy, atmospheric haze are administered, national product oil upgrade to state five and mark
Standard, it is increasing to the demand of clean gasoline.In order to meet market needs, the economy of methanol enterprise is improved, the present invention carries
The method for producing gasoline is realized under the action of catalyst for a kind of methanol, liquefied petroleum gas, circulating air, heavy hydrocarbon.
The content of the invention
The technical problems to be solved by the invention are：Using methanol as primary raw material, under the action of catalyst, catalytic reforming
Heavy hydrocarbons content is reduced, increases gasoline content, improves the selectivity of preparing gasoline by methanol, improves the economy of preparing gasoline by methanol device.
The present invention takes following technical proposals to solve above-mentioned technical problem：
A kind of method that methanol prepares gasoline, includes the following steps：
A. material benzenemethanol feeding methanol booster is boosted, is re-fed into preheating device preheating, is then sent into vapourizing unit
Vaporization, is then fed into superheater and carries out Overheating Treatment；
B. overheat after methanol enter catalytic reactor carry out catalytic reaction, the catalytic reactor must controlling reaction temperature,
Pressure and mass space velocity；
C. the output object input cooling device of the catalytic reactor is cooled down, is then fed into gas-oil-water three phase separation
Device carries out isolated circulating air, oil mixture is mixed with water compound, and the oil mixture handles to obtain into stabilizer
Raw gasoline product and liquefied petroleum gas, the raw gasoline product enter Cutting Tap further isolated gasoline products and heavy hydrocarbon production
Product, the aqueous mixture make outer row's processing.
Preferably, the product of catalytic reactor described in step C first flows through the superheater before cooling device is entered
Cooled down, product after cooling is partly into the vapourizing unit and preheating device and further cools down, and another part enters
Circulating air heating unit further cools down, and two parts product after cooling, which mixes, enters back into the cooling device.
Preferably, the isolated liquefied petroleum gas of stabilizer is recycled to liquefied petroleum gas booster liter in the step C
Pressure, then converges to be sent into afterwards in the vapourizing unit together and vaporizes with the methanol of preheated device preheating in the step A again,
Methanol and liquefied petroleum gas after vaporization are re-fed into the superheater and carry out Overheating Treatment, methanol and liquefied petroleum after overheat
Gas enters the catalytic reactor and carries out catalytic reaction.
Preferably, the step C is sent to cycle compressor by the circulating air of the gas-oil-water three-phase separator output
Device boosting, the circulating air heating devices heat, then converge with the methanol described in step A through vaporization and liquefied petroleum gas again
After be sent into the superheater and together carry out Overheating Treatment, be finally sent into the catalytic reactor and carry out catalytic reaction.
Preferably, molecular sieve catalyst is housed in catalytic reactor in the step C, the catalytic reactor is divided into two
Section：Controlling reaction temperature is 400~420 DEG C in first segment catalytic reaction process, and pressure is 2.0~2.5 MPa, mass space velocity
For 20~50 h-1；Controlling reaction temperature is 390~410 DEG C in second segment catalytic reaction process, and pressure is 2.0~2.5
MPa, mass space velocity are 1.0~1.5 h-1。
The isolated heavier hydrocarbon products of Cutting Tap are sent to after heavy hydrocarbon circulating pump in the step C is delivered to the catalysis again
Heavy hydrocarbon pressure described in the input terminal cycling and reutilization of the second segment of reactor boosts to 1.9~2.0 MPa；The cycle compressor
Circulating air after the boosting that device produces is delivered to the input terminal of the second segment of the catalytic reactor, to reduce system temperature.
Preferably, the purity of the material benzenemethanol in the step A is：90.0~99.9%, its pressure after boosting is 2.0
~2.5 MPa；The pressure that the circulating air of the step C enters after cycle compressor device boosting is 2.0~2.5 MPa.
The temperature of superheater is 300 DEG C ± 10 DEG C in the step A.The cooling temperature of cooling device in the step C is 45 DEG C
±5℃；Do outer row's processing in the superpressure part that the step C is sent to the circulating air of cycle compressor device boosting.
A kind of system of preparing gasoline by methanol, it is characterised in that including：By methanol booster, preheating device, vapourizing unit, mistake
The main preparation system that thermal, catalytic reactor, cooling device, gas-oil-water three-phase separator, stabilizer, Cutting Tap are linked in sequence
System.
Material benzenemethanol boosts through the methanol booster, preheating device preheating, vapourizing unit heating vaporization, superheater into
Row overheat, then send to the catalytic reactor and carries out catalytic reaction, is cooled down subsequently into the cooling device, finally by described
Gas-oil-water three-phase separator output circulating air, oil mixture are mixed with water compound.The oil mixture enters stabilizer
Processing obtains raw gasoline product and liquefied petroleum gas, and the raw gasoline product enters Cutting Tap further isolated gasoline products
And heavier hydrocarbon products, the aqueous mixture make outer row's processing.
Preferably, between the catalytic reactor output terminal and the input terminal of cooling device, the catalytic reactor is defeated
Outlet first connects the superheater, is further divided into two branches, and a branch is the vapourizing unit, preheating device, cooling dress
Put the thermal cycle passage that the thermal energy of composition recycles；Another branch is circulating air heating unit, cooling device composition
The thermal cycle passage that thermal energy recycles.The product of the catalytic reactor output first flows through the superheater and is cooled down, cold
But the product after is partly into the vapourizing unit and preheating device and further cools down, and another part adds into the circulating air
Thermal further cools down, and two parts product after cooling, which mixes, enters back into the cooling device.
Preferably, the liquefied petroleum gas port of export of the stabilizer, liquefied petroleum gas booster, the vapourizing unit enter
Mouth end, which is linked in sequence, forms the bypath system of liquefied petroleum gas cycling and reutilization.The isolated liquefied petroleum gas of the stabilizer
The boosting of liquefied petroleum gas booster is recycled to, then converges again with the methanol of preheated device preheating and is sent into the vaporization afterwards together
Vaporized in device.
Preferably, the gas-between the gas phase outlet of oil-water three-phase separator and the input terminal of superheater and connecing follows
Ring air pressure compression apparatus and the circulating air heating unit are filled with being formed by the gas-oil-water three-phase separator, cycle compressor
Put, the bypath system for the circulating air cycling and reutilization that circulating air heating unit and superheater are formed.The circulation pneumatic transmission is extremely
The boosting of cycle compressor device, circulating heater heating, then again with being sent after the methanol of vaporization and liquefied petroleum gas converge
Enter superheater and together carry out Overheating Treatment, be then sent into catalytic reactor and carry out catalytic reaction, last re-enter institute
State cooling device and carry out cycling and reutilization.
Preferably, molecular sieve catalyst is housed, the catalytic reactor is divided into two sections in the catalytic reactor：First
Controlling reaction temperature is 400~420 DEG C in section catalytic reaction process, and pressure is 2.0~2.5 MPa, and mass space velocity is 20~50
h-1；Controlling reaction temperature is 390~410 DEG C in second segment catalytic reaction process, and pressure is 2.0~2.5 MPa, mass space velocity
For 1.0~1.5 h-1。
Second segment input terminal, heavy hydrocarbon circulating pump, the output terminal of Cutting Tap of the catalytic reactor, which are linked in sequence, forms weight
The bypath system of hydrocarbon cycling and reutilization.The heavier hydrocarbon products that the Cutting Tap produces first are sent to the processing of heavy hydrocarbon circulating pump, after processing
It is admitted to the input terminal cycling and reutilization of the catalytic reactor second segment.
The second segment input terminal of the catalytic reactor connects the output terminal of the cycle compressor device, the circulating air
Circulating air after the boosting that compression set produces is sent to the input terminal of the catalytic reactor second segment, to reduce system temperature
Degree.
The beneficial effects of the invention are as follows：Realize recycling for heavy hydrocarbon and liquefied petroleum gas in preparing gasoline by methanol device, carry
The selectivity of high methanol gasoline, gasoline recovery rate are improved to 95%（The prior art only has 75%）, add high added value gasoline
The yield of product, improves the economy of methanol hydrocarbon, there is higher economic value and social benefit.
Brief description of the drawings
Fig. 1 is a kind of process flow chart of the method and system of preparing gasoline by methanol of the embodiment of the present invention；
The meaning that each sequence number represents in attached drawing is as follows：
1st, methanol booster；2nd, liquefied petroleum gas booster；3rd, cycle compressor device；4th, preheating device；5th, vapourizing unit；6、
Circulating air heating unit；7th, superheater；8th, catalytic reactor；9th, cooling device；10th, gas-oil-water three-phase separator；11st, it is steady
Determine tower；12nd, Cutting Tap；13rd, heavy hydrocarbon circulating pump.
Embodiment
In order to make the purpose , technical scheme and advantage of the present invention be clearer, with reference to the accompanying drawings and embodiments, it is right
The present invention is further elaborated.
As shown in Figure 1, the present invention realizes that the system of preparing gasoline by methanol includes：By methanol booster 1, preheating device 4, vapour
5, superheater 7, catalytic reactor 8, cooling device 9, gas-oil-water three-phase separator 10, stabilizer 11, Cutting Tap are put in makeup
The 12 main preparation systems being linked in sequence.
The liquefied petroleum gas port of export of stabilizer 11, liquefied petroleum gas booster 2, the vapourizing unit 5 is further included to enter
Mouth end, which is linked in sequence, forms the bypath system of liquefied petroleum gas cycling and reutilization.
Further include between the gas phase outlet of gas-oil-water three-phase separator 10 and the input terminal of superheater 7 and connect circulation
Air pressure compression apparatus 3 and circulating air heating unit 6 with formed by the gas-oil-water three-phase separator 10, cycle compressor device 3,
The bypath system for the circulating air cycling and reutilization that circulating air heating unit 6 and superheater 7 are formed.
Between 8 output terminal of catalytic reactor and the input terminal of cooling device 9,8 output terminal of catalytic reactor
The superheater 7 is first connected, is further divided into two branches, a branch is the vapourizing unit 5, preheating device 4, cooling device
The thermal cycle passage that the thermal energy of 9 compositions recycles；Another branch is the circulating air heating unit 6, the composition of cooling device 9
The thermal cycle passage that thermal energy recycles.
Molecular sieve catalyst is housed, the catalytic reactor is divided into two sections in the catalytic reactor 8：It is catalyzed in first segment
Controlling reaction temperature is 400~420 DEG C in reaction process, and pressure is 2.0~2.5 MPa, and mass space velocity is 20~50 h-1；
Controlling reaction temperature is 390~410 DEG C in second segment catalytic reaction process, and pressure is 2.0~2.5 MPa, mass space velocity 1.0
~1.5 h-1。
Second segment input terminal, heavy hydrocarbon circulating pump 13, the output terminal of Cutting Tap 12 of the catalytic reactor 8 are linked in sequence group
Into the bypath system of heavy hydrocarbon cycling and reutilization.The second segment input terminal of the catalytic reactor 8 connects the cycle compressor dress
Put 3 output terminal.
Based on the above-mentioned system for realizing preparing gasoline by methanol, the present invention realizes that the process of preparing gasoline by methanol includes following step
Suddenly：
A. material benzenemethanol is sent into methanol booster 1 to boost, is re-fed into preheating device 4 and preheats, be then sent into vapourizing unit
Vaporized in 5, be then fed into superheater 7 and carry out Overheating Treatment；
B. the methanol after overheating enters catalytic reactor 8 and carries out catalytic reaction, and the catalytic reactor 8 must control reaction temperature
Degree, pressure and mass space velocity；
C. by the output object of the catalytic reactor 8, first flow through the superheater 7 and cooled down, product one after cooling
Divide and further cooled down into the vapourizing unit 5 and preheating device 4, it is further cold that another part enters circulating air heating unit 6
But, two parts product after cooling, which mixes, enters back into the cooling device 9 and cools down, and is then fed into gas-oil-water three-phase separate
Carry out isolated circulating air from device 10, oil mixture is mixed with water compound, the oil mixture enter stabilizer 11 at
Reason obtains raw gasoline product and liquefied petroleum gas, and the raw gasoline product enters the further isolated gasoline products of Cutting Tap 12
And heavier hydrocarbon products, the aqueous mixture make outer row's processing.The isolated liquefied petroleum gas of stabilizer 11 is recycled to liquefaction stone
Oil gas booster 2 boosts, and then converges again with the methanol of the preheated preheating of device 4 in the step A and is sent into the vapour afterwards together
Makeup vaporizes in putting 5, and the methanol and liquefied petroleum gas after vaporization are re-fed into the superheater 7 and carry out Overheating Treatment, after overheat
Methanol and liquefied petroleum gas enter the catalytic reactor 8 carry out catalytic reaction.Gas-oil-the water three-phase separator 10 is defeated
The circulating air gone out is sent to that cycle compressor device 3 boosts, the circulating air heating unit 6 heats, then again with described in step A
The superheater 7 is sent into after the methanol and liquefied petroleum gas of vaporization converge and together carries out Overheating Treatment, finally described in feeding
Catalytic reaction is carried out in catalytic reactor 8.The isolated heavier hydrocarbon products of Cutting Tap 12 are sent to defeated again after heavy hydrocarbon circulating pump 13
Send the input terminal cycling and reutilization of the second segment to the catalytic reactor 8.Following after the boosting that cycle compressor device 3 produces
Ring gas is delivered to the input terminal of the second segment of the catalytic reactor 8, to reduce system temperature.It is described to be sent to cycle compressor
Do outer row's processing in the superpressure part for the circulating air that device 3 boosts.
Embodiment 1：Requirement and the above method according to the technological process shown in Fig. 1, control 100 kg/h of methanol flow,
Methanol purity is 99.9%.500 kg/h of circulating air flow, circulating air composition:H210%, CH460%, C2H410%, C2H6 20%。
It is 1.9 MPa to circulate heavy hydrocarbon boost pressure.It is 20h that 8 first segment of catalytic reactor, which controls mass space velocity,-1, temperature is 420 DEG C, pressure
Power is 2.5 MPa；It is 1.5 h of speed that second segment, which controls quality sky,-1, temperature is 390 DEG C, and pressure is under the process conditions of 2.5 MPa.
Reaction result：12 isolated gasoline products of Cutting Tap, reach 5 92 gasoline quality standard of state through analyzing gasoline products.
Embodiment 2：Requirement and the above method according to the technological process shown in Fig. 1, control 200 kg/h of methanol flow,
Methanol purity is 95.4%.900 kg/h of circulating air flow, circulating air composition:H210%, CH460%, C2H410%, C2H6 20%。
It is 2.0 MPa to circulate heavy hydrocarbon boost pressure.It is 35h that 8 first segment of catalytic reactor, which controls mass space velocity,-1, temperature is 400 DEG C, pressure
Power is 2.2 MPa；It is 1.2 h of speed that second segment, which controls quality sky,-1, temperature is 400 DEG C, and pressure is under the process conditions of 2.3 MPa.
Reaction result：12 isolated gasoline products of Cutting Tap, reach 5 92 gasoline quality standard of state through analyzing gasoline products.
Embodiment 3：Requirement and the above method according to the technological process shown in Fig. 1, control 200 kg/h of methanol flow,
Methanol purity is 90.0%.900 kg/h of circulating air flow, circulating air composition:H210%, CH460%, C2H410%, C2H6 20%。
It is 1.9 MPa to circulate heavy hydrocarbon boost pressure.It is 50h that 8 first segment of catalytic reactor, which controls mass space velocity,-1, temperature is 410 DEG C, pressure
Power is 2.0 MPa；It is 1.0 h of speed that second segment, which controls quality sky,-1, temperature is 410 DEG C, and pressure is under the process conditions of 2.0 MPa.
Reaction result：12 isolated gasoline products of Cutting Tap, reach 5 92 gasoline quality standard of state through analyzing gasoline products.
Above content is that a further detailed description of the present invention in conjunction with specific preferred embodiments, it is impossible to is assert
The specific implementation of the present invention is confined to these explanations.For general technical staff of the technical field of the invention,
On the premise of not departing from present inventive concept, some simple deduction or replace can also be made, should all be considered as belonging to the present invention's
Protection domain.
Claims (17)
1. a kind of method that methanol prepares gasoline, it is characterised in that include the following steps：
A. material benzenemethanol is sent into methanol booster（1）Boost, be re-fed into preheating device（4）Preheating, is then sent into vaporization
Device（5）Middle vaporization, is then fed into superheater（7）Carry out Overheating Treatment；
B. the methanol after overheating enters catalytic reactor（8）Carry out catalytic reaction, the catalytic reactor（8）It must control anti-
Answer temperature, pressure and mass space velocity；
C. by the catalytic reactor（8）Output object input cooling device（9）Cooled down, be then fed into gas-oil-water three
Phase separator（10）Carry out isolated circulating air, oil mixture is mixed with water compound, the oil mixture entrance stabilization
Tower（11）Processing obtains raw gasoline product and liquefied petroleum gas, and the raw gasoline product enters Cutting Tap（12）Further separate
To gasoline products and heavier hydrocarbon products, the aqueous mixture makees outer row's processing.
2. the method that methanol according to claim 1 prepares gasoline, it is characterised in that：Catalytic reactor described in step C（8）
Product into cooling device（9）Before, the superheater is first flowed through（7）Cooled down, a product part after cooling
Into the vapourizing unit（5）And preheating device（4）Further cooling, another part enter circulating air heating unit（6）Into one
Step cooling, two parts product after cooling, which mixes, enters back into the cooling device（9）.
3. the method that methanol according to claim 1 prepares gasoline, it is characterised in that：Stabilizer in the step C（11）
Isolated liquefied petroleum gas is recycled to liquefied petroleum gas booster（2）Boosting, then again with it is preheated in the step A
Device（4）The methanol of preheating converges is sent into the vapourizing unit afterwards together（5）Middle vaporization, methanol and liquefied petroleum gas after vaporization
It is re-fed into the superheater（7）Overheating Treatment is carried out, the methanol and liquefied petroleum gas after overheat enter the catalytic reactor
（8）Carry out catalytic reaction.
4. the method that methanol according to claim 1 prepares gasoline, it is characterised in that：The step C by the gas-oil-
Water three-phase separator（10）The circulating air of output is sent to cycle compressor device（3）Boosting, the circulating air heating unit（6）
Heating, the superheater is sent into after then converging again with the methanol and liquefied petroleum gas described in step A through vaporization（7）Together into
Row Overheating Treatment, is finally sent into the catalytic reactor（8）Middle carry out catalytic reaction.
5. the method that methanol according to claim 1 prepares gasoline, it is characterised in that：Catalytic reactor in the step C
（8）In molecular sieve catalyst is housed, the catalytic reactor is divided into two sections：The control reaction temperature in first segment catalytic reaction process
Spend for 400~420 DEG C, pressure is 2.0~2.5 MPa, and mass space velocity is 20~50 h-1；In second segment catalytic reaction process
Controlling reaction temperature is 390~410 DEG C, and pressure is 2.0~2.5 MPa, and mass space velocity is 1.0~1.5 h-1。
6. the method that methanol according to any one of claims 1 to 6 prepares gasoline, it is characterised in that：Cut in the step C
Cut tower（12）Isolated heavier hydrocarbon products are sent to heavy hydrocarbon circulating pump（13）It is delivered to the catalytic reactor again afterwards（8）
Two sections of input terminal cycling and reutilization；The heavy hydrocarbon pressure boosts to 1.9~2.0 MPa.
7. the method that methanol according to any one of claims 1 to 6 prepares gasoline, it is characterised in that：The circulation air pressure
Compression apparatus（3）Circulating air after the boosting of generation is delivered to the catalytic reactor（8）Second segment input terminal, to reduce body
It is temperature.
8. the method that methanol according to any one of claims 1 to 3 prepares gasoline, it is characterised in that：In the step A
The purity of material benzenemethanol is：90.0~99.9%, the pressure after it boosts is 2.0~2.5 MPa；The circulating air of the step C into
Enter the cycle compressor device（3）Pressure after boosting is 2.0~2.5 MPa.
9. the method that methanol according to claim 1 prepares gasoline, it is characterised in that：Superheater in the step A（7）
Temperature be 300 DEG C ± 10 DEG C.
10. the method that methanol according to any one of claims 1 to 4 prepares gasoline, it is characterised in that：In the step C
Cooling device（9）Cooling temperature be 45 DEG C ± 5 DEG C；The step C is sent to cycle compressor device（3）The circulation of boosting
Do outer row's processing in the superpressure part of gas.
A kind of 11. system of preparing gasoline by methanol, it is characterised in that：Including by methanol booster（1）, preheating device（4）, vaporization dress
Put（5）, superheater（7）, catalytic reactor（8）, cooling device（9）, gas-oil-water three-phase separator（10）, stabilizer（11）
And Cutting Tap（12）The main preparation system being linked in sequence；
Material benzenemethanol is through the methanol booster（1）Boosting, preheating device（4）Preheating, vapourizing unit（5）Heating vaporization, overheat
Device（7）Overheated, then sent to the catalytic reactor（8）Catalytic reaction is carried out, subsequently into the cooling device（9）
Cooling, finally by the gas-oil-water three-phase separator（10）Output circulating air, oil mixture are mixed with water compound；
The oil mixture enters stabilizer（11）Processing obtains raw gasoline product and liquefied petroleum gas, the raw gasoline product
Into Cutting Tap（12）Further isolated gasoline products and heavier hydrocarbon products, the aqueous mixture make outer row's processing.
12. the system of preparing gasoline by methanol according to claim 11, it is characterised in that：In the catalytic reactor（8）It is defeated
Outlet and cooling device（9）Input terminal between, the catalytic reactor（8）Output terminal first connects the superheater（7）, then
It is divided into two branches, a branch is the vapourizing unit（5）, preheating device（4）, cooling device（9）The thermal energy of composition is sharp again
Thermal cycle passage；Another branch is circulating air heating unit（6）, the cooling device（9）The thermal energy of composition recycles
Thermal cycle passage；
The catalytic reactor（8）The product of output first flows through the superheater（7）Cooled down, product one after cooling
Divide and enter the vapourizing unit（5）And preheating device（4）Further cooling, another part enter the circulating air heating unit
（6）Further cooling, two parts product after cooling, which mixes, enters back into the cooling device（9）.
13. the system of preparing gasoline by methanol according to claim 11, it is characterised in that：The stabilizer（11）Liquefaction stone
Oil gas vent end, liquefied petroleum gas booster（2）, the vapourizing unit（5）Arrival end be linked in sequence composition liquefied petroleum gas
The bypath system of cycling and reutilization；
The stabilizer（11）Isolated liquefied petroleum gas is recycled to liquefied petroleum gas booster（2）Boosting, then again and
Preheated device（4）The methanol of preheating converges is sent into the vapourizing unit afterwards together（5）Middle vaporization.
14. the system of preparing gasoline by methanol according to claim 11, it is characterised in that：Including the gas-oil-water three-phase separate
From device（10）Gas phase outlet and superheater（7）Input terminal between and connect cycle compressor device（3）With the circulation
Gas heating unit（6）To be formed by the gas-oil-water three-phase separator（10）, cycle compressor device（3）, circulating air heating
Device（6）And superheater（7）The bypath system of the circulating air cycling and reutilization formed；
The pneumatic transmission that circulates is to cycle compressor device（3）Boosting, circulating heater（6）Heating, then again with through vaporization
Methanol and liquefied petroleum gas are sent into superheater after converging（7）Overheating Treatment is together carried out, is then sent into catalytic reactor（8）In
Carry out catalytic reaction, cooling device described in last re-enter（9）Carry out cycling and reutilization.
A kind of 15. system of preparing gasoline by methanol according to claim 11, it is characterised in that：The catalytic reactor（8）
In molecular sieve catalyst, the catalytic reactor are housed（8）It is divided into two sections：The control reaction temperature in first segment catalytic reaction process
Spend for 400~420 DEG C, pressure is 2.0~2.5 MPa, and mass space velocity is 20~50 h-1；In second segment catalytic reaction process
Controlling reaction temperature is 390~410 DEG C, and pressure is 2.0~2.5 MPa, and mass space velocity is 1.0~1.5 h-1。
A kind of 16. system of preparing gasoline by methanol according to claim 11, it is characterised in that：The catalytic reactor（8）
Second segment input terminal, heavy hydrocarbon circulating pump（13）, Cutting Tap（12）Output terminal be linked in sequence composition heavy hydrocarbon cycling and reutilization
Bypath system；
The Cutting Tap（12）The heavier hydrocarbon products of generation are first sent to heavy hydrocarbon circulating pump（13）Processing, is admitted to described urge after processing
Change reactor（8）The input terminal cycling and reutilization of second segment.
A kind of 17. system of preparing gasoline by methanol according to claim 15, it is characterised in that：The catalytic reactor（8）
Second segment input terminal connect the cycle compressor device（3）Output terminal, the cycle compressor device（3）The liter of generation
Circulating air after pressure is sent to the catalytic reactor（8）The input terminal of second segment, to reduce system temperature.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746877A (en) * | 2011-04-20 | 2012-10-24 | 中国石油化工股份有限公司 | Method for preparing gasoline from methanol |
| CN105001900A (en) * | 2015-07-31 | 2015-10-28 | 赛鼎工程有限公司 | Technology of synthesizing gasoline by coke oven gas through methyl alcohol |
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2016
- 2016-10-19 CN CN201610906036.5A patent/CN107964417A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746877A (en) * | 2011-04-20 | 2012-10-24 | 中国石油化工股份有限公司 | Method for preparing gasoline from methanol |
| CN105001900A (en) * | 2015-07-31 | 2015-10-28 | 赛鼎工程有限公司 | Technology of synthesizing gasoline by coke oven gas through methyl alcohol |
Non-Patent Citations (1)
| Title |
|---|
| 王永刚等: "《煤化工工艺学》", 30 September 2014, 中国矿业大学出版社 * |
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Application publication date: 20180427 |