CN110252210A - It is a kind of suitable for newly-built and improving alteration methanol synthesizing process and device - Google Patents
It is a kind of suitable for newly-built and improving alteration methanol synthesizing process and device Download PDFInfo
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- CN110252210A CN110252210A CN201910530215.7A CN201910530215A CN110252210A CN 110252210 A CN110252210 A CN 110252210A CN 201910530215 A CN201910530215 A CN 201910530215A CN 110252210 A CN110252210 A CN 110252210A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The first methanol column and the second methanol column are filled into respectively by a certain percentage suitable for newly-built and improving alteration methanol synthesizing process, including the first methanol-fueled CLC and the second methanol-fueled CLC, virgin gas the present invention provides a kind of.The present invention also provides a kind of devices suitable for above-mentioned methanol synthesizing process.The present invention passes through the production intensity of two methanol columns of reasonable distribution, improves catalyst service life and efficiency, improves conversion per pass, reduces recycle ratio, has obvious practicability and economic benefit.
Description
Technical field
The present invention relates to chemical process, especially a kind of technique for greatly improving methanol production capacity and device.
Background technique
Industrial methanol is by CO, CO2And H2It is anti-that methanol-fueled CLC is carried out under certain temperature, pressure and catalyst action
It should produce.
Methanol synthesis reaction is a kind of strongly exothermic reversible reaction, and every reaction 1%CO adiabatic temperature rise is up to 32 DEG C, and catalyst
It the use of temperature is 210 DEG C~280 DEG C, thus the heat needs of reaction process are quickly removed, to guarantee catalyst bed suitable
Temperature range in.Currently, industrially removing reaction heat by burying heat exchanger tube in catalyst bed to realize, pass through water evaporation
It is a kind of simple and effective temperature control means that byproduct steam, which takes away reaction heat,.
Methanol-fueled CLC is finally controlled by balance, and conversion per pass will not be very high, therefore isolates the process gas after crude carbinol
Some is mixed after being compressed as circulating air by circulator with virgin gas, constitutes a circulation loop, and it is total to improve system
Conversion ratio.
Enlarged methanol scale effect is obvious, and in order to improve methanol project economy, newly-built methanol device tends to enlargement,
Built methanol device then needs to carry out capacity expansion revamping.Patent EP0790226B1 provide a kind of enlarged methanol production method and
System, virgin gas and the laggard level-one pipe-type water-cooling reactor of circulating air are then gas-cooled reactor into second level, manage in virgin gas with
The gaseous mixture of circulating air carries out moving heat, and the gas after second order reaction carries out gas-liquid separation after cooling, separates one gas circulation.This
Kind methanol synthesis loop has that front and back stages reaction production intensity distribution is unreasonable, production water-cooled reactor early period production
Intensity is high, and air cooling reactor production intensity is low, and outlet temperature is low, and the methanol in gas can be condensed in catalyst bed；After production
Phase water-cooled reactor catalyst activity fast decay, production intensity decline, air cooling reactor production intensity improves, anti-due to being gas-cooled
Answer device heat transfer efficiency low, bed temperature is not easy to control, causes by-product to increase, while follow-up process air cooler, water cooler load
Increase.Large size process for methanol production and system described in patent 105399604A, front and back stages reactor all use water cooling anti-
Two-stage water cooling is passed sequentially through after answering device, virgin gas to mix with circulating air to react.It is anti-that this methanol synthesis loop equally exists two-stage
The unreasonable problem of intensity distribution should be produced, production first-stage reactor early period production intensity is high, and catalyst bed hot(test)-spot temperature is high,
Cause by-product high, catalyst life is short；It produces later period first-stage reactor and produces strength reduction, second reactor production intensity mentions
Height, catalyst bed hot(test)-spot temperature increase, also result in by-product height and catalyst life is short.In patent 107382665A description
A kind of methanol synthesizing process and device, first reactor is water-cooled reactor, and second reactor is air cooling reactor or water cooling
Reactor controls second reactor by valve A simply by valve B control first reactor inlet temperature at 200-240 DEG C
Hot(test)-spot temperature is no more than 250 DEG C, and the virgin gas that A valve introduces second reactor accounts for the 25-0mol% of virgin gas total amount, this methanol
Synthesis loop equally exists production first reactor early period production intensity height, and catalyst bed hot(test)-spot temperature is high, and by-product is high, urges
The agent service life is short；It produces later period second reactor production intensity to improve, by-product height and catalyst life are short, two-stage reaction production
The unreasonable problem of intensity distribution.
In addition, methanol synthesizer is a circulation loop, in original system Equipment Foundations, especially in recycle compressor
Under conditions of performance is difficult to improve, methanol device transformation is carried out, improves methanol output, this is also a technological difficulties.
Summary of the invention
In view of the above-mentioned problems, the present invention provides a kind of suitable for newly-built and improving alteration methanol synthesizing process, including
First system for methanol synthesis and secondary methanol synthesis system, virgin gas fill into the first methanol-fueled CLC system by certain allocation proportion respectively
System and the second system for methanol synthesis, the allocation proportion is preferably 3: 1~1: 2, and optimal allocation proportion is 2: 1~1: 1.
Be applicable in above-mentioned methanol synthesizing process newly-built methanol device include fresh air compressor, circulator, First Heat Exchanger,
Second heat exchanger, third heat exchanger, detoxification slot, the first methanol column, the second methanol column, air cooler, methanol separator, the first vapour
Packet and the second drum are sequentially connected the second heat exchanger, third heat exchanger and the first methanol column after the circulator, and described is new
Fresh air compressor is sequentially connected with First Heat Exchanger, detoxification slot, and the detoxification slot outlet is divided into two tunnels, connects the first first all the way
Alcohol tower into tower tube road, another way connect the second methanol column into tower tube road, the export pipeline of first methanol column is successively
Connect third heat exchanger and the second methanol column, the export pipeline of second methanol column is sequentially connected the second heat exchanger, air-cooled
Device, water cooler and methanol separator, first methanol column and each external drum of the second methanol column.
Raw material virgin gas exchanges heat after virgin gas compressor boost with a part of second methanol column exhaust gas, then goes detoxification
Slot detoxification.Virgin gas after detoxification is divided into two strands, one is mixed with the circulating air after heat exchange, carries out subsequently into the first methanol column
Methanol synthesis reaction.It is mixed after exhaust gas heat cycles gas with another burst of virgin gas, carries out methanol subsequently into the second methanol column
Synthetic reaction.It is cooling through air cooler and water cooler after exhaust gas heating process gas, after isolating crude carbinol into methanol separator, one
Part is discharged as periodic off-gases, remaining goes circulator to be pressurized as circulating air.
The improving alteration methanol device for being applicable in above-mentioned methanol synthesizing process includes fresh air compressor, joint compressor, the
One heat exchanger, the second heat exchanger, third heat exchanger, detoxification slot, the first methanol column, the second methanol column, air cooler, separating methanol
Device, the first drum and the second drum, the fresh air pipe of raw material are divided into two tunnels and are separately connected joint compressor and fresh air compressor,
The second heat exchanger, third heat exchanger and the first methanol column, the virgin gas compression are sequentially connected after the joint compressor
Machine is sequentially connected with First Heat Exchanger, detoxification slot, and the detoxification slot outlet is divided into two tunnels, connects the first methanol-fueled CLC all the way
Into tower tube road, another way connect the second methanol column into tower tube road, the export pipeline of first methanol column is sequentially connected the
The export pipeline of three heat exchangers and the second methanol column, second methanol column is sequentially connected the second heat exchanger, air cooler, water cooling
Device and methanol separator, first methanol column and each external drum of the second methanol column.
Raw material virgin gas is divided into two strands, one increases with antenatal fresh tolerance equivalent, process joint compressor compresses section is proposed
It is mixed in cylinder after pressure with circulating air, into joint compressor cycle section pressurization, then successively goes out tower with the second methanol column of a part
Gas and the first methanol column exhaust gas exchange heat, and change after another stock-traders' know-how virgin gas compressor boost with remaining second methanol column exhaust gas
Heat, then go detoxification slot detoxification.Virgin gas after detoxification, a part is mixed with the compressor outlet gas of combining after heat exchange, into the
One methanol column carries out methanol synthesis reaction, and exhaust gas mixes after exchanging heat with remaining virgin gas, subsequently into the second methanol column into
Row methanol synthesis reaction.It is cooling through air cooler and water cooler after exhaust gas heating process gas, thick first is isolated into methanol separator
After alcohol, a part is discharged as periodic off-gases, remaining goes joint compressor cycle section to be pressurized as circulating air.
As a preferred embodiment, the first methanol column in above-mentioned methanol synthesizer has two, while carrying out methanol conjunction
At reaction.
First methanol column and the second methanol column is preferred water-cooled reactor, respectively matches a drum.
Present invention process produces intensity by reasonable distribution, improves catalyst life and efficiency, by improving conversion per pass
Rate reduces recycle ratio, greatly improves methanol production capacity, specifically:
1. virgin gas fills into the first methanol column and the second methanol column by certain allocation proportion respectively, preferred allocation proportion is
3: 1~1: 2, optimal allocation proportion is 2: 1~1: 1, and reasonable distribution produces intensity.
2. Optimization of Heat Exchanger Networks, the second methanol column exhaust gas is divided into two strands, heats respectively to circulating air and virgin gas,
First methanol column exhaust gas carries out reheating to circulating air, meets the requirement of the first methanol column inlet temperature of stabilizer.
3. virgin gas is reached by the heating of the second methanol column exhaust gas and is divided to two strands after catalyst activity temperature again, virgin gas is the
One methanol column entrance and circulating air are mixed in the second methanol column entrance and the free ratio of exhaust gas, use early period according to catalyst
Different with the later period, the production intensity that the first methanol column and the second methanol column internal accelerator are controlled by adjusting virgin gas ratio is put down
27~50% virgin gases are filled into the second methanol column as produced early period by weighing apparatus, arrive the first methanol column catalyst production Intensity Transfer
Second methanol column reduces the first methanol column hot spot and by-product, keeps the catalyst life of the first methanol column and the second methanol identical.
4. two water-cooled reactors are arranged, two reactors respectively match a drum, control the producing steam pressure of two reactors
Power.
5. in reforming technology process, part detoxifying agent is loaded on the first methanol column top.
Virgin gas by being filled into the first, second methanol column by present invention process process respectively in proportion, and reasonable distribution two
Methanol column produces intensity, and two methanol column reaction bed temperatures is made to be at most suitable temperature range, reduces by-product, improves
Catalyst service life and efficiency.Second methanol column controls lower producing steam temperature, to reduce reactor outlet temperature, pushes
Reaction balance moves to right, and improves conversion per pass, reduces recycle ratio, has obvious practicability and economic benefit.
Detailed description of the invention:
Fig. 1 is the newly-built methanol device flow diagram using methanol synthesizing process of the present invention.
Fig. 2 is the improving alteration methanol device flow diagram using methanol synthesizing process of the present invention.
Fig. 3 is the schematic device that two the first methanol columns are used in methanol synthesizer of the present invention.
Description of symbols:
A- combines the second heat exchanger of compressor E2- E3- third heat exchanger the first methanol column of R1-
Fresh the second methanol column of the air compressor E1- First Heat Exchanger R2- h- air cooler of e-
I- water cooler j- methanol separator k- the first drum the second drum of 1-
P- third drum m- circulator n- detoxification slot R1a- the first methanol a tower
R1b- the first methanol b tower
Specific embodiment
Embodiment 1
Implement by Fig. 1 process flow, by taking methanol produces 700000 tons of techniques per year as an example.
Virgin gas mole composition are as follows: CO 29.18%, CO22.49%, H267.61%, N20.37%, CH4
0.34%.1 flow of raw material virgin gas is 203275Nm3/ h is pressurized to 8.1MPa through fresh air compressor e.Virgin gas is compressed out
The logistics 22 of machine e exchanges heat through the exhaust gas 15 of First Heat Exchanger E1 and wherein one second methanol column R2 to 200 DEG C, then goes detoxification
Slot n detoxification.It is two strands that logistics 23 after detoxification slot n detoxification, which is divided to, and logistics 24 and logistics 7, gas flow are respectively 54885Nm3/
H and 148390Nm3/h.Circulating air 3 is pressurized to 8.1MPa through circulator m.Out the logistics 4 of circulator m through the second heat exchanger E2 with
The exhaust gas 13 of another the second methanol column of stock R2 exchanges heat to 200 DEG C, then goes out tower through third heat exchanger E3 and the first methanol column R1
Gas 9 exchanges heat to 225 DEG C.Logistics 7 is mixed with the logistics 6 after third heat exchanger E3 heating, and mixed 8 temperature of logistics is 213
℃.Logistics 8 enters the first methanol column R1 and carries out methanol synthesis reaction, out 235 DEG C of 9 temperature of tower logistics.Logistics 9 is through third heat exchanger
It is mixed after E3 heated stream 5 with logistics 24, mixed 11 temperature of logistics is 213 DEG C.Logistics 11 enter the second methanol column R2 into
Row methanol synthesis reaction, 12 temperature of tower logistics is 215 DEG C out.Logistics 12 is divided into two strands, logistics 13 and logistics 15.Logistics 13 is through
Two heat exchanger E2 heated streams 4, through First Heat Exchanger E1 heated stream 22, the two streams after heat exchange are remixed for logistics 15, are mixed
Closing 17 temperature of logistics is 135 DEG C.Logistics 17 enters methanol separator j after air cooler h and water cooler i are cooled to 40 DEG C and carries out gas
Liquid separation, liquid phase crude carbinol 20 remove methanol rectification, and it is two strands that gaseous stream 34, which is divided to, circulating air 3 and periodic off-gases 35, and circulating air 3 flows
Amount is 304912Nm3/ h, circulating air 3 go circulator m to be pressurized.First methanol column R1 and the second methanol column R2 is respectively provided with
One drum k and the second drum 1.
First methanol column R1 catalyst loading 36m3, producing steam pressure 2.5MPa, the second methanol column R2 catalyst loading
36m3, producing steam pressure 1.6MPa, recycle ratio 1.5, by this technique, CO conversion per pass 88.3%, CO2Conversion per pass
42.1%, produce 71.43 ten thousand tons of methanol per year.
Embodiment 2
Implement by Fig. 2 process flow, by taking methanol produces 700000 tons of technique early periods per year as an example.
Virgin gas mole composition are as follows: CO 29.18%, CO22.49%, H267.61%, N20.37%, CH4
0.34%.1 flow of raw material virgin gas is 203275Nm3/ h, is divided into two strands, and logistics 2 and logistics 21, gas flow are respectively
78262Nm3/ h and 125013Nm3/h.Logistics 2 mixes in cylinder after the pressurization of the joint compression section compressor a with circulating air 3, then
Combined compressor a circulation section and is pressurized to 8.1MPa.Out combine compressor a logistics 4 through heat exchanger E2 with wherein one second
The exhaust gas 13 of methanol column R2 exchanges heat to 200 DEG C, then exchanges heat through the exhaust gas 9 of heat exchanger E3 and the first methanol column R1 to 215 DEG C.
Logistics 21 is pressurized to 8.1MPa through fresh air compressor e.The logistics 22 of fresh air compressor e is through heat exchanger E1 and another stock the out
The exhaust gas 15 of dimethanol tower R2 exchanges heat to 200 DEG C, then goes detoxification slot n detoxification.It is two that logistics 23 after detoxification slot n detoxification, which is divided to,
Stock, logistics 24 and logistics 7, gas flow are respectively 70007Nm3/ h and 55006Nm3/h.Logistics 7 with through heat exchanger E3 heating after
Logistics 6 mix, mixed 8 temperature of logistics be 213 DEG C.Logistics 8 enters the first methanol column R1 and carries out methanol synthesis reaction, out
228 DEG C of 9 temperature of tower logistics.Logistics 9 mixes after heat exchanger E3 heated stream 5 with logistics 24, and mixed 11 temperature of logistics is
213℃.Logistics 11 enters the second methanol column R2 and carries out methanol synthesis reaction, and 12 temperature of tower logistics is 217 DEG C out.Logistics 12 is divided into
Two strands, logistics 13 and logistics 15.Logistics 13 is through heat exchanger E2 heated stream 4, and logistics 15 is through heat exchanger E1 heated stream 22, heat exchange
Two streams afterwards remix, and 17 temperature of mixture flow is 135 DEG C.Logistics 17 is after air cooler h and water cooler i are cooled to 40 DEG C
Gas-liquid separation is carried out into methanol separator j, liquid phase crude carbinol 20 removes methanol rectification, and it is two strands that gaseous stream 34, which is divided to, circulating air 3
With periodic off-gases 35,3 flow of circulating air is 304912Nm3/ h, circulating air 3 go joint compressor a circulation section to be pressurized.First first
Alcohol tower R1 and the second methanol column R2 are respectively provided with the first drum k and the second drum 1.
First methanol column catalyst loading 36m3, producing steam pressure 2.5MPa, the second methanol column catalyst loading 36m3, produce
Steam pressure 1.5MPa, recycle ratio 1.5 mention production. art by this, and CO conversion per pass is up to 89.9%, CO2Conversion per pass reaches
47.0%, produce 72.74 ten thousand tons of methanol per year.
Embodiment 3
Implement by Fig. 2 process flow, by taking methanol produces 700000 tons of technique early periods per year as an example.
Virgin gas mole composition are as follows: CO 29.18%, CO22.49%, H267.61%, N20.37%, CH4
0.34%.1 flow of raw material virgin gas is 203275Nm3/ h is pressurized to 8.1MPa through fresh air compressor e.Virgin gas is compressed out
The logistics 22 of machine e exchanges heat through the exhaust gas 15 of heat exchanger E1 and wherein one second methanol column R2 to 200 DEG C, then removes detoxification slot n
Detoxification.It is two strands that logistics 23 after detoxification slot n detoxification, which is divided to, and logistics 24 and logistics 7, gas flow are respectively 67690Nm3/ h and
135585Nm3/h.Circulating air 3 is pressurized to 8.1MPa through circulator m.The logistics 4 of circulator m is through heat exchanger E2 and another stock the out
The exhaust gas 13 of dimethanol tower R2 exchanges heat to 200 DEG C, then through the exhaust gas 9 of heat exchanger E3 and the first methanol column R1 heat exchange to 220
℃.Logistics 7 is mixed with the logistics 6 after heat exchanger E3 heating, and mixed 8 temperature of logistics is 213 DEG C.Logistics 8 enters first
Methanol column R1 carries out methanol synthesis reaction, out 230 DEG C of 9 temperature of tower logistics.Logistics 9 after heat exchanger E3 heated stream 5 with logistics
24 mixing, mixed 11 temperature of logistics are 213 DEG C.Logistics 11 enters the second methanol column R2 and carries out methanol synthesis reaction, out tower
12 temperature of logistics is 216 DEG C.Logistics 12 is divided into two strands, logistics 13 and logistics 15.Logistics 13 is through heat exchanger E2 heated stream 4, object
Through heat exchanger E1 heated stream 22, the two streams after heat exchange remix stream 15, and 17 temperature of mixture flow is 135 DEG C.Logistics 17
Enter methanol separator j after air cooler h and water cooler i are cooled to 40 DEG C and carry out gas-liquid separation, liquid phase crude carbinol 20 removes methanol
Rectifying, it is two strands that gaseous stream 34, which is divided to, circulating air 3 and periodic off-gases 35, and 3 flow of circulating air is 304912Nm3/ h, circulating air 3 are gone
Circulator m is pressurized.First methanol column R1 and the second methanol column R2 are respectively provided with the first drum k and the second drum 1.
First methanol column catalyst loading 36m3, producing steam pressure 2.5MPa, the second methanol column catalyst loading 36m3, produce
Steam pressure 1.6MPa, recycle ratio 1.5 mention production. art by this, and CO conversion per pass is up to 90.1%, CO2Conversion per pass reaches
47.0%, produce 72.75 ten thousand tons of methanol per year.
Embodiment 4
Implement by Fig. 2 process flow, by taking methanol produces 700000 tons of technique later periods per year as an example.
Virgin gas mole composition are as follows: CO 29.18%, CO22.49%, H267.61%, N20.37%, CH4
0.34%.1 flow of raw material virgin gas is 203275Nm3/ h is pressurized to 8.1MPa through fresh air compressor e.Virgin gas is compressed out
The logistics 22 of machine e exchanges heat through the exhaust gas 15 of heat exchanger E1 and wherein one second methanol column R2 to 200 DEG C, then removes detoxification slot n
Detoxification.It is two strands that logistics 23 after detoxification slot n detoxification, which is divided to, and logistics 24 and logistics 7, gas flow are respectively 135585Nm3/h
And 67690Nm3/h.Circulating air 3 is pressurized to 8.1MPa through circulator m.The logistics 4 of circulator m is through heat exchanger E2 and another stock out
The exhaust gas 13 of second methanol column R2 exchanges heat to 200 DEG C, then extremely through the heat exchange of the exhaust gas 9 of heat exchanger E3 and the first methanol column R1
230℃.Logistics 7 is mixed with the logistics 6 after heat exchanger E3 heating, and mixed 8 temperature of logistics is 221 DEG C.Logistics 8 respectively into
Enter the first methanol a tower R1a and the second methanol b tower R1b and carry out methanol synthesis reaction, the logistics of two towers is mixed into 9 temperature of logistics out
259℃.Logistics 9 mixes after heat exchanger E3 heated stream 5 with logistics 24, and mixed 11 temperature of logistics is 233 DEG C.Logistics 11
Methanol synthesis reaction is carried out into the second methanol column R2,12 temperature of tower logistics is 239 DEG C out.Logistics 12 is divided into two strands, logistics 13
With logistics 15.Logistics 13 is through heat exchanger E2 heated stream 4, two strand objects of the logistics 15 through heat exchanger E1 heated stream 22, after heat exchange
Stream remixes, and 17 temperature of mixture flow is 138 DEG C.Logistics 17 is after air cooler h and water cooler i are cooled to 40 DEG C into methanol point
Gas-liquid separation is carried out from device j, liquid phase crude carbinol 20 removes methanol rectification, and it is two strands that gaseous stream 34, which is divided to, circulating air 3 and periodic off-gases
35,3 flow of circulating air is 304912Nm3/ h, circulating air 3 go circulator m to be pressurized.First methanol column R1 and the second methanol column
R2 is respectively provided with the first drum k and the second drum 1.
First methanol a tower catalyst loading 18m3, the first methanol b tower catalyst loading 18m3, producing steam pressure 4.0MPa,
Second methanol column catalyst loading 36m3, producing steam pressure 1.6MPa, recycle ratio 1.5 mentions production. art, CO conversion per pass by this
Up to 74.2%, CO2Conversion per pass produces 71.35 ten thousand tons of methanol per year up to 27.2%.
Embodiment 5
Implement by Fig. 3 process flow, by taking methanol produces 700000 tons of technique early periods per year as an example.
Virgin gas mole composition are as follows: CO 29.18%, CO22.49%, H267.61%, N20.37%, CH4
0.34%.1 flow of raw material virgin gas is 203275Nm3/ h is pressurized to 8.1MPa through fresh air compressor e.Virgin gas is compressed out
The logistics 22 of machine e exchanges heat through the exhaust gas 15 of First Heat Exchanger E1 and wherein one second methanol column R2 to 200 DEG C, then goes detoxification
Slot n detoxification.It is two strands that logistics 23 after detoxification slot n detoxification, which is divided to, and logistics 24 and logistics 7, gas flow are respectively 54885Nm3/
H and 148390Nm3/h.Circulating air 3 is pressurized to 8.1MPa through circulator m.Out the logistics 4 of circulator m through the second heat exchanger E2 with
The exhaust gas 13 of another the second methanol column of stock R2 exchanges heat to 200 DEG C, then goes out tower through third heat exchanger E3 and the first methanol column R1
Gas 9 exchanges heat to 225 DEG C.Logistics 7 is mixed with the logistics 6 after third heat exchanger E3 heating, and mixed 8 temperature of logistics is 213
℃.It is two strands that logistics 8, which divides, respectively enters the first methanol a tower R1a and the first methanol b tower R1b while carrying out methanol synthesis reaction,
Two strands of the first methanol a tower R1a and the first methanol b tower R1b go out tower logistics and merge into logistics 9 out, and 235 DEG C of temperature.Logistics 9 is through
It is mixed after three heat exchanger E3 heated streams 5 with logistics 24, mixed 11 temperature of logistics is 213 DEG C.Logistics 11 enters the second first
Alcohol tower R2 carries out methanol synthesis reaction, and 12 temperature of tower logistics is 215 DEG C out.Logistics 12 is divided into two strands, logistics 13 and logistics 15.Object
Stream 13 is through the second heat exchanger E2 heated stream 4, and logistics 15 is through First Heat Exchanger E1 heated stream 22, and the two streams after heat exchange are again
Mixing, 17 temperature of mixture flow are 135 DEG C.Logistics 17 enters methanol separator after air cooler h and water cooler i are cooled to 40 DEG C
J carries out gas-liquid separation, and liquid phase crude carbinol 20 removes methanol rectification, and it is two strands that gaseous stream 34, which is divided to, and circulating air 3 and periodic off-gases 35 follow
3 flow of ring gas is 304912Nm3/ h, circulating air 3 go circulator m to be pressurized.First methanol a tower R1a and the first methanol b tower
R1b is respectively provided with third drum p and the first drum k, the second methanol column R2 is furnished with the second drum 1.
First methanol column R1 catalyst loading 36m3, producing steam pressure 2.5MPa, the second methanol column R2 catalyst loading
36m3, producing steam pressure 1.6MPa, recycle ratio 1.5, by this technique, CO conversion per pass 88.3%, CO2Conversion per pass
42.1%, produce 71.43 ten thousand tons of methanol per year.
Claims (9)
1. a kind of close suitable for newly-built and improving alteration methanol synthesizing process, including the first system for methanol synthesis and the second methanol
At system, it is characterised in that: virgin gas fills into the first system for methanol synthesis and the second methanol-fueled CLC by certain allocation proportion respectively
System.
2. as described in claim 1 be suitable for newly-built and improving alteration methanol synthesizing process, it is characterised in that: point
It is 3: 1~1: 2 with ratio.
3. as claimed in claim 2 be suitable for newly-built and improving alteration methanol synthesizing process, it is characterised in that: point
It is 2: 1~1: 1 with ratio.
4. as described in claim 1 be suitable for newly-built and improving alteration methanol synthesizing process, it is characterised in that: newly-built methanol
In device, the virgin gas is divided into two strands, one is mixed with the circulating air after heat exchange, subsequently into the first system for methanol synthesis
Methanol synthesis reaction is carried out, is mixed after the exhaust gas heat cycles gas of the first system for methanol synthesis with another burst of virgin gas, then
Methanol synthesis reaction is carried out into the second system for methanol synthesis.
5. as described in claim 1 be suitable for newly-built and improving alteration methanol synthesizing process, it is characterised in that: built methanol
In device improving alteration device, the raw material virgin gas is divided into two strands, one with propose antenatal fresh tolerance equivalent, pass through
It is mixed in cylinder after the pressurization of joint compressor compresses section with circulating air, into joint compressor cycle section pressurization, then successively with one
The heat exchange of the exhaust gas of the exhaust gas of part the second methanol system and the first system for methanol synthesis, another stock-traders' know-how virgin gas through pressurization,
It is divided into two parts after heat exchange detoxification, a part combines the mixing of compressor outlet gas with after heat exchange, into the first methanol-fueled CLC system
System carries out methanol synthesis reaction, and the exhaust gas of the first system for methanol synthesis mixes after exchanging heat with another part virgin gas, then
Methanol synthesis reaction is carried out into the second system for methanol synthesis.
6. as described in claim 1 be suitable for newly-built and improving alteration methanol synthesizing process, it is characterised in that: described the
One methanol column and the second methanol column are water-cooled reactor, and the water-cooled reactor respectively matches a drum.
7. a kind of methanol synthesizer for methanol synthesizing process as claimed in claim 4, including fresh air compressor, circulation
Machine, First Heat Exchanger, the second heat exchanger, third heat exchanger, detoxification slot, the first methanol column, the second methanol column, air cooler, water cooling
Device, methanol separator, the first drum and the second drum, it is characterised in that: be sequentially connected after the circulator the second heat exchanger,
Third heat exchanger and level-one methyl alcohol synthetic reactor, the fresh air compressor is sequentially connected with First Heat Exchanger, detoxification slot, described
The outlet of detoxification slot be divided into two tunnels, connect all the way the first methanol column into tower tube road, another way connect the second methanol column into tower
Pipeline, the export pipeline of first methanol column are sequentially connected third heat exchanger and the second methanol column, second methanol
The export pipeline of tower is sequentially connected the second heat exchanger, air cooler, water cooler and methanol separator, first methanol column and
Each external drum of dimethanol tower.
8. a kind of methanol synthesizer for methanol synthesizing process as claimed in claim 5, including fresh air compressor, joint
Compressor, First Heat Exchanger, the second heat exchanger, third heat exchanger, detoxification slot, the first methanol column, the second methanol column, air cooler,
Water cooler, methanol separator, the first drum and the second drum, it is characterised in that: the fresh air pipe of raw material is divided into two tunnels and connects respectively
Connect joint compressor and fresh air compressor, be sequentially connected after the joint compressor the second heat exchanger, third heat exchanger and
First methanol column, the fresh air compressor are sequentially connected with First Heat Exchanger, detoxification slot, and the detoxification slot outlet is divided into
Two tunnels, connect all the way the first methanol column into tower tube road, another way connect the second methanol column into tower tube road, first first
The export pipeline of alcohol tower is sequentially connected third heat exchanger and the second methanol column, and the export pipeline of second methanol column successively connects
Connect the second heat exchanger, air cooler, water cooler and methanol separator, first methanol column and the second methanol column each external one
Drum.
9. methanol synthesizer as claimed in claim 7 or 8, it is characterised in that: first methanol column is two, simultaneously
Carry out methanol-fueled CLC.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201910530215.7A CN110252210A (en) | 2019-06-11 | 2019-06-11 | It is a kind of suitable for newly-built and improving alteration methanol synthesizing process and device |
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| CN201910530215.7A CN110252210A (en) | 2019-06-11 | 2019-06-11 | It is a kind of suitable for newly-built and improving alteration methanol synthesizing process and device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110665244A (en) * | 2019-10-09 | 2020-01-10 | 万华化学集团股份有限公司 | Gas phase reaction device and method for preparing dicyclohexylamine |
| CN111440049A (en) * | 2020-04-15 | 2020-07-24 | 陕西聚能新创煤化科技有限公司 | High-efficient methyl alcohol synthesis system |
-
2019
- 2019-06-11 CN CN201910530215.7A patent/CN110252210A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110665244A (en) * | 2019-10-09 | 2020-01-10 | 万华化学集团股份有限公司 | Gas phase reaction device and method for preparing dicyclohexylamine |
| CN110665244B (en) * | 2019-10-09 | 2021-10-22 | 万华化学集团股份有限公司 | Gas phase reaction device and method for preparing dicyclohexylamine |
| CN111440049A (en) * | 2020-04-15 | 2020-07-24 | 陕西聚能新创煤化科技有限公司 | High-efficient methyl alcohol synthesis system |
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