CN104387230B - A kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam - Google Patents
A kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam Download PDFInfo
- Publication number
- CN104387230B CN104387230B CN201410675418.2A CN201410675418A CN104387230B CN 104387230 B CN104387230 B CN 104387230B CN 201410675418 A CN201410675418 A CN 201410675418A CN 104387230 B CN104387230 B CN 104387230B
- Authority
- CN
- China
- Prior art keywords
- gas
- flash steam
- methyl alcohol
- valve
- inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Use a method for the device process methyl alcohol flash steam of process methyl alcohol flash steam, it relates to a kind of method processing flash steam.The object of the invention is will solve in existing methanol process and produce methyl alcohol flash steam, there is the cost height of recycling methyl alcohol flash steam and directly methyl alcohol flash steam is discharged in air the problem causing resource waste and pollution environment in existing method.Device comprises purified gas inlet tube, valve, process furnace, fuel gas surge tank, oxygen and water vapour inlet pipe, converter, compressor, synthetic tower, water cooler, flash drum, exhaust-valve, flash steam separator, methanol outlet pipe, Heat Exchanger in Circulating Water System and inlet tower gas interchanger; Method: one, adjusting gas flow; Two, reforming gas is prepared in reaction; Three, methanol-fueled CLC reaction; Four, cool, be separated, the method for the process methyl alcohol flash steam namely completed.The present invention can obtain a kind of device processing methyl alcohol flash steam and the method using its process methyl alcohol flash steam.
Description
Technical field
The present invention relates to a kind of method processing flash steam.
Background technology
Methyl alcohol flash steam enters in flash drum at the isolated methyl alcohol of methanol separator, pressure is down to low pressure rapidly from high pressure, be dissolved in mixed gas abrupt release in methyl alcohol out, comprising methane, ethane, carbon monoxide, carbonic acid gas, hydrogen, methanol gas, this gaseous constituent is complicated, has higher thermal value.Containing 12% ~ 18% methane gas from the synthesizing methanol purified gas that purification section comes, this part gas is rare gas element for synthesizing methanol, do not participate in building-up reactions, and affect reaction efficiency, methane gas wherein and oxygen water vapour react by partial oxidation workshop section, produce the active principle of carbon monoxide, carbonic acid gas, hydrogen synthesizing methanol.
The methyl alcohol that existing method is produced mainly utilizes lurgi gasifier pressure gasification process, in lurgi gasifier pressure gasification process methanol process, the methyl alcohol flash steam produced, methyl alcohol flash steam complicated component, recycle difficulty, but wherein also containing methane, carbon monoxide, the high heat value gas such as methyl alcohol, recycling problem is good terms of settlement never, usually two kinds are had to the treatment process of this part flash steam: first method is: flash steam pressure is low, if enter methanol synthetic system need increase a flash steam compressor newly, be compressed to more than 2MPa, by the carbon monoxide in flash steam, carbonic acid gas, the active principle of hydrogen synthesizing methanol utilizes, but methane wherein, ethane, the inert components such as nitrogen affect synthesis efficiency, and a newly-increased compressor power cost consumption increases, analyze from economic benefit aspect, there is no practical significance, second method is: flash steam directly enters air after flash drum decompression, not only wastes resource but also causes certain influence to environment.
Summary of the invention
The object of the invention is will solve in existing methanol process and produce methyl alcohol flash steam, there is the cost height of recycling methyl alcohol flash steam and directly methyl alcohol flash steam be discharged in air the problem causing resource waste and pollution environment in existing method, and provides a kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam.
A kind of device processing methyl alcohol flash steam comprises purified gas inlet tube, the first valve, the second valve, the 3rd valve, process furnace, fuel gas surge tank, oxygen and water vapour inlet pipe, converter, compressor, synthetic tower, water cooler, flash drum, exhaust-valve, flash steam separator, methanol outlet pipe, Heat Exchanger in Circulating Water System and inlet tower gas interchanger;
Heat exchanger tube and flame distributor is provided with in described process furnace; Described purified gas inlet tube is connected with the inlet end of fuel gas surge tank with the inlet end of heat exchanger tube respectively; Be provided with the first valve between purified gas inlet tube and heat exchanger tube, between purified gas inlet tube and fuel gas surge tank, be provided with the second valve; The exit end of fuel gas surge tank is connected with flame distributor, and is provided with the 3rd valve between fuel gas surge tank and flame distributor; The exit end of heat exchanger tube is connected with the entrance end of converter with water vapour inlet pipe inlet end respectively with oxygen; The exit end of converter is connected with the inlet end of Heat Exchanger in Circulating Water System, and the exit end of Heat Exchanger in Circulating Water System is connected with the inlet end of compressor; The exit end of compressor is connected with the inlet end of inlet tower gas interchanger, and the exit end of inlet tower gas interchanger is connected with the inlet end of synthetic tower, and the exit end of synthetic tower is connected with the inlet end of water cooler; The exit end of water cooler is connected with the inlet end of flash drum; The top exit end of flash drum is connected with the inlet end of flash steam separator; The top exit end of flash steam separator is connected with fuel gas surge tank; The outlet at bottom end of flash drum is connected with methanol outlet pipe respectively with the outlet at bottom end of flash steam separator.
Process a method for methyl alcohol flash steam, specifically complete according to the following steps:
One, adjusting gas flow: first open the first valve, the second valve and the 3rd valve, regulate the first valve, the gas flow making the purification coal gas containing 12% ~ 18% methane gas enter into heat exchanger tube from purified gas inlet tube by the first valve is 111800Nm
3/ h; Regulate the second valve, the gas flow making the purification coal gas containing 12% ~ 18% methane gas enter into fuel gas surge tank from purified gas inlet tube by the second valve is 1130Nm
3/ h; Regulate the 3rd valve, the gas flow making the gas in fuel gas surge tank enter into flame distributor is 2240m
3/ h;
Two, reforming gas is prepared in reaction: flame distributor naked light burns the gas entered from fuel gas surge tank, and by purification heated by gas intrafascicular for Tube Sheet of Heat Exchanger, being warming up to 550 DEG C, is then that the purification coal gas of 550 DEG C enters into converter by temperature; Oxygen and water vapour are entered into converter from oxygen and water vapour inlet pipe, temperature is the purification coal gas of 550 DEG C and the oxygen entered from oxygen and water vapour inlet pipe and the combustion chamber mixed firing of water vapour on converter top, and then the beds through converter bottom, carry out the steam reforming reaction of hydro carbons, obtain the reforming gas that temperature is 1002 DEG C;
Three, methanol-fueled CLC reaction: temperature is that the reforming gas of 1002 DEG C enters into Heat Exchanger in Circulating Water System and cools, temperature drops to 40 DEG C, then compressor is entered into, the pressure of reforming gas is risen to 8.3MPa by compressor, then enter into inlet tower gas interchanger, temperature rises to 225 DEG C, then enters into the adiabatic catalytic oxidant layer of tubulation in synthetic tower from synthetic tower top, flow through tubulation inner catalyst bed after intensification from top to bottom and carry out methanol-fueled CLC reaction, obtain reaction gas;
Four, cool, be separated: reaction gas out, enters into water cooler and is cooled to 40 DEG C, then isolate crude carbinol from water cooler bottom synthetic tower, and crude carbinol is discharged from the bottom of methyl alcohol water cooler, enters into flash drum; Reforming gas in water cooler from the exit end at the top of water cooler out, enters into compressor, re-starts building-up reactions; The crude carbinol entering into flash drum discharges methyl alcohol flash steam through flash drum decompression, methyl alcohol flash steam is discharged from the upper end of flash drum, enters into flash steam separator, then after flash steam separator is separated, discharge from the upper end of flash steam separator, enter into fuel gas surge tank; The methyl alcohol separated through flash drum and flash steam separator enters into methanol outlet pipe, discharges, the method for the process methyl alcohol flash steam namely completed through methanol outlet pipe.
Advantage of the present invention: in the present invention, the flow of the methane flash steam that flash steam separator upper end produces is 2000m
3/ h, be high heating value mixed gas, methane flash steam enters into fuel gas surge tank, mix in fuel gas surge tank with purification coal gas, enter into process furnace, burn as raw material, methane flash steam comprises methane, ethane, carbon monoxide, hydrogen, is 25.6MJ/m with reference to calorific value
3burning has fine heats, compare sublimate heated by gas efficiency high a lot, purification coal gas is 13.5MJ/ cubic meter with reference to calorific value, decrease the usage quantity of purification coal gas, bring certain economic benefit, per hour supplement 2000 cubic metres purification coal gas burn in process furnace, by the calculating of purification coal gas 2.5 yuan, per hourly save 5000 yuans, bring certain economic benefit, and methane flash steam gas does not enter in air, environment is not had any impact, there is certain environmental benefit.
The present invention can obtain a kind of device processing methyl alcohol flash steam and the method using its process methyl alcohol flash steam.
Embodiment
Embodiment one: present embodiment is that a kind of device processing methyl alcohol flash steam comprises purified gas inlet tube 1, first valve 2, second valve 3, the 3rd valve 4, process furnace 5, fuel gas surge tank 6, oxygen and water vapour inlet pipe 7, converter 8, compressor 9, synthetic tower 10, water cooler 11, flash drum 12, exhaust-valve 13, flash steam separator 14, methanol outlet pipe 15, Heat Exchanger in Circulating Water System 16 and inlet tower gas interchanger 17;
Heat exchanger tube 5-1 and flame distributor 5-2 is provided with in described process furnace 5; Described purified gas inlet tube 1 is connected with the inlet end of fuel gas surge tank 6 with the inlet end of heat exchanger tube 5-1 respectively; Be provided with the first valve 2 between purified gas inlet tube 1 and heat exchanger tube 5-1, between purified gas inlet tube 1 and fuel gas surge tank 6, be provided with the second valve 3; The exit end of fuel gas surge tank 6 is connected with flame distributor 5-2, and is provided with the 3rd valve 4 between fuel gas surge tank 6 and flame distributor 5-2; The exit end of heat exchanger tube 5-1 is connected with the entrance end of converter 8 with water vapour inlet pipe 7 inlet end respectively with oxygen; The exit end of converter 8 is connected with the inlet end of Heat Exchanger in Circulating Water System 16, and the exit end of Heat Exchanger in Circulating Water System 16 is connected with the inlet end of compressor 9; The exit end of compressor 9 is connected with the inlet end of inlet tower gas interchanger 17, and the exit end of inlet tower gas interchanger 17 is connected with the inlet end of synthetic tower 10, and the exit end of synthetic tower 10 is connected with the inlet end of water cooler 11; The exit end of water cooler 11 is connected with the inlet end of flash drum 12; The top exit end of flash drum 12 is connected with the inlet end of flash steam separator 14; The top exit end of flash steam separator 14 is connected with fuel gas surge tank 6; The outlet at bottom end of flash drum 12 is connected with methanol outlet pipe 15 respectively with the outlet at bottom end of flash steam separator 14.
The advantage of present embodiment: in present embodiment, the flow of the methane flash steam that flash steam separator 14 upper end produces is 2000m
3/ h, be high heating value mixed gas, methane flash steam enters into fuel gas surge tank 6, mix in fuel gas surge tank 6 with purification coal gas, enter into process furnace 5, burn as raw material, methane flash steam comprises methane, ethane, carbon monoxide, hydrogen, is 25.6MJ/m with reference to calorific value
3burning has fine heats, compare sublimate heated by gas efficiency high a lot, purification coal gas is 13.5MJ/ cubic meter with reference to calorific value, decrease the usage quantity of purification coal gas, bring certain economic benefit, per hour supplement 2000 cubic metres purification coal gas burn in process furnace, by the calculating of purification coal gas 2.5 yuan, per hourly save 5000 yuans, bring certain economic benefit, and methane flash steam gas does not enter in air, environment is not had any impact, there is certain environmental benefit.
Present embodiment can obtain a kind of device processing methyl alcohol flash steam and the method using its process methyl alcohol flash steam.
Embodiment two: present embodiment with the difference of embodiment one is: the exit end at water cooler 11 top is connected with the inlet end at compressor 9 top.Other are identical with embodiment one.
Embodiment three: the difference of present embodiment and embodiment one or two is: be provided with exhaust-valve 13 between flash drum 12 and flash steam separator 14.Other are identical with embodiment one or two.
Embodiment four: the difference of present embodiment and embodiment one to three is: be provided with tubulation in synthetic tower 10, tubulation is built with catalyzer.Other are identical with embodiment one to three.
Embodiment five: present embodiment is that a kind of method processing methyl alcohol flash steam specifically completes according to the following steps:
One, adjusting gas flow: first open the first valve 2, second valve 3 and the 3rd valve 4, regulate the first valve 2, the gas flow making the purification coal gas containing 12% ~ 18% methane gas enter into heat exchanger tube 5-1 from purified gas inlet tube 1 by the first valve 2 is 111800Nm
3/ h; Regulate the second valve 3, the gas flow making the purification coal gas containing 12% ~ 18% methane gas enter into fuel gas surge tank 6 from purified gas inlet tube 1 by the second valve 3 is 1130Nm
3/ h; Regulate the 3rd valve 4, the gas flow making the gas in fuel gas surge tank 6 enter into flame distributor 5-2 is 2240m
3/ h;
Two, reforming gas is prepared in reaction: flame distributor 5-2 naked light burns the gas entered from fuel gas surge tank 6, and by the purification heated by gas in heat exchanger tube 5-1, being warming up to 550 DEG C, is then that the purification coal gas of 550 DEG C enters into converter 8 by temperature; Oxygen and water vapour are entered into converter 8 from oxygen and water vapour inlet pipe 7, temperature is the purification coal gas of 550 DEG C and the oxygen entered from oxygen and water vapour inlet pipe 7 and the combustion chamber mixed firing of water vapour on converter 8 top, and then the beds through converter 8 bottom, carry out the steam reforming reaction of hydro carbons, obtain the reforming gas that temperature is 1002 DEG C;
Three, methanol-fueled CLC reaction: temperature is that the reforming gas of 1002 DEG C enters into Heat Exchanger in Circulating Water System 16 cooling, temperature drops to 40 DEG C, then compressor 9 is entered into, the pressure of reforming gas is risen to 8.3MPa by compressor 9, then enter into inlet tower gas interchanger 17, temperature rises to 225 DEG C, then enters into the adiabatic catalytic oxidant layer of tubulation in synthetic tower 10 from synthetic tower 10 top, flow through tubulation inner catalyst bed after intensification from top to bottom and carry out methanol-fueled CLC reaction, obtain reaction gas;
Four, cool, be separated: reaction gas out, enters into water cooler 11 and is cooled to 40 DEG C, then isolate crude carbinol from water cooler 11 bottom synthetic tower 10, and crude carbinol is discharged from the bottom of methyl alcohol water cooler 11, enters into flash drum 12; Reforming gas in water cooler 11 from the exit end at the top of water cooler 11 out, enters into compressor 9, re-starts building-up reactions; The crude carbinol entering into flash drum 12 discharges methyl alcohol flash steam through flash drum 12 decompression, methyl alcohol flash steam is discharged from the upper end of flash drum 12, enter into flash steam separator 14, again after flash steam separator 14 is separated, discharge from the upper end of flash steam separator 14, enter into fuel gas surge tank 6; The methyl alcohol separated through flash drum 12 and flash steam separator 14 enters into methanol outlet pipe 15, discharges through methanol outlet pipe 15, the method for the process methyl alcohol flash steam namely completed.
Embodiment six: the difference of present embodiment and embodiment five is: in step 2, temperature is that the contents on dry basis of methane in the reforming gas of 1002 DEG C is less than 0.5%.Other are identical with embodiment five.
Embodiment seven: the difference of present embodiment and embodiment five or six is: in step 2, temperature is the composition of the reforming gas of 1002 DEG C is CO
2, CO, H
2and H
2o.Other are identical with embodiment five or six.
Embodiment eight: the difference of present embodiment and embodiment five to seven is: the main component of the methyl alcohol flash steam described in step 4 is carbonic acid gas, carbon monoxide, methane, ethane, hydrogen, nitrogen, first alcohol and water; Wherein the content of carbonic acid gas is 11.7% ~ 12.5%, the content of carbon monoxide is 3.7% ~ 4.6%, the content of methane is 38.3% ~ 40.5%, the content of ethane is 2.4% ~ 3.6%, the content of hydrogen is 33.8% ~ 38.3%, the content of nitrogen is 0.7% ~ 0.8%, and the content of methyl alcohol is 6.3% ~ 7.2%, and the content of water is 0.18%.Other are identical with embodiment five to seven.
Embodiment nine: the difference of present embodiment and embodiment five to eight is: in step 4, methyl alcohol flash steam is discharged from the upper end of flash steam separator 14, the gas flow entering into fuel gas surge tank 6 is 2000m
3/ h.Other are identical with embodiment five to eight.
Embodiment ten: the difference of present embodiment and embodiment five to nine is: the reaction gas in step 3 is CH
3oH and H
2o.Other are identical with embodiment five to nine.
Adopt following verification experimental verification beneficial effect of the present invention:
Test one: a kind of device processing methyl alcohol flash steam comprises purified gas inlet tube 1, first valve 2, second valve 3, the 3rd valve 4, process furnace 5, fuel gas surge tank 6, oxygen and water vapour inlet pipe 7, converter 8, compressor 9, synthetic tower 10, water cooler 11, flash drum 12, exhaust-valve 13, flash steam separator 14, methanol outlet pipe 15, Heat Exchanger in Circulating Water System 16 and inlet tower gas interchanger 17;
Heat exchanger tube 5-1 and flame distributor 5-2 is provided with in described process furnace 5; Described purified gas inlet tube 1 is connected with the inlet end of fuel gas surge tank 6 with the inlet end of heat exchanger tube 5-1 respectively; Be provided with the first valve 2 between purified gas inlet tube 1 and heat exchanger tube 5-1, between purified gas inlet tube 1 and fuel gas surge tank 6, be provided with the second valve 3; The exit end of fuel gas surge tank 6 is connected with flame distributor 5-2, and is provided with the 3rd valve 4 between fuel gas surge tank 6 and flame distributor 5-2; The exit end of heat exchanger tube 5-1 is connected with the entrance end of converter 8 with water vapour inlet pipe 7 inlet end respectively with oxygen; The exit end of converter 8 is connected with the inlet end of Heat Exchanger in Circulating Water System 16, and the exit end of Heat Exchanger in Circulating Water System 16 is connected with the inlet end of compressor 9; The exit end of compressor 9 is connected with the inlet end of inlet tower gas interchanger 17, and the exit end of inlet tower gas interchanger 17 is connected with the inlet end of synthetic tower 10, and the exit end of synthetic tower 10 is connected with the inlet end of water cooler 11; The exit end of water cooler 11 is connected with the inlet end of flash drum 12; The top exit end of flash drum 12 is connected with the inlet end of flash steam separator 14; The top exit end of flash steam separator 14 is connected with fuel gas surge tank 6; The outlet at bottom end of flash drum 12 is connected with methanol outlet pipe 15 respectively with the outlet at bottom end of flash steam separator 14.
Use a kind of method processing the device process methyl alcohol flash steam of methyl alcohol flash steam, specifically complete according to the following steps:
One, adjusting gas flow: first open the first valve 2, second valve 3 and the 3rd valve 4, regulate the first valve 2, the gas flow making the purification coal gas containing 12% ~ 18% methane gas enter into heat exchanger tube 5-1 from purified gas inlet tube 1 by the first valve 2 is 111800Nm
3/ h; Regulate the second valve 3, the gas flow making the purification coal gas containing 12% ~ 18% methane gas enter into fuel gas surge tank 6 from purified gas inlet tube 1 by the second valve 3 is 1130Nm
3/ h; Regulate the 3rd valve 4, the gas flow making the gas in fuel gas surge tank 6 enter into flame distributor 5-2 is 2240m
3/ h;
Two, reforming gas is prepared in reaction: flame distributor 5-2 naked light burns the gas entered from fuel gas surge tank 6, and by the purification heated by gas in heat exchanger tube 5-1, being warming up to 550 DEG C, is then that the purification coal gas of 550 DEG C enters into converter 8 by temperature; Oxygen and water vapour are entered into converter 8 from oxygen and water vapour inlet pipe 7, temperature is the purification coal gas of 550 DEG C and the oxygen entered from oxygen and water vapour inlet pipe 7 and the combustion chamber mixed firing of water vapour on converter 8 top, and then the beds through converter 8 bottom, carry out the steam reforming reaction of hydro carbons, obtain the reforming gas that temperature is 1002 DEG C;
Three, methanol-fueled CLC reaction: temperature is that the reforming gas of 1002 DEG C enters into Heat Exchanger in Circulating Water System 16 cooling, temperature drops to 40 DEG C, then compressor 9 is entered into, the pressure of reforming gas is risen to 8.3MPa by compressor 9, then enter into inlet tower gas interchanger 17, temperature rises to 225 DEG C, then enters into the adiabatic catalytic oxidant layer of tubulation in synthetic tower 10 from synthetic tower 10 top, flow through tubulation inner catalyst bed after intensification from top to bottom and carry out methanol-fueled CLC reaction, obtain reaction gas;
Four, cool, be separated: reaction gas out, enters into water cooler 11 and is cooled to 40 DEG C, then isolate crude carbinol from water cooler 11 bottom synthetic tower 10, and crude carbinol is discharged from the bottom of methyl alcohol water cooler 11, enters into flash drum 12; Reforming gas in water cooler 11 from the exit end at the top of water cooler 11 out, enters into compressor 9, re-starts building-up reactions; The crude carbinol entering into flash drum 12 discharges methyl alcohol flash steam through flash drum 12 decompression, methyl alcohol flash steam is discharged from the upper end of flash drum 12, enter into flash steam separator 14, again after flash steam separator 14 is separated, discharge from the upper end of flash steam separator 14, enter into fuel gas surge tank 6; The methyl alcohol separated through flash drum 12 and flash steam separator 14 enters into methanol outlet pipe 15, discharges through methanol outlet pipe 15, the method for the process methyl alcohol flash steam namely completed.
In this test, the flow of the methane flash steam that flash steam separator 14 upper end produces is 2000m
3/ h, be high heating value mixed gas, methane flash steam enters into fuel gas surge tank 6, mix in fuel gas surge tank 6 with purification coal gas, enter into process furnace 5, burn as raw material, methane flash steam comprises methane, ethane, carbon monoxide, hydrogen, is 25.6MJ/m with reference to calorific value
3burning has fine heats, compare sublimate heated by gas efficiency high a lot, purification coal gas is 13.5MJ/ cubic meter with reference to calorific value, decrease the usage quantity of purification coal gas, bring certain economic benefit, per hour supplement 2000 cubic metres purification coal gas burn in process furnace, by the calculating of purification coal gas 2.5 yuan, per hourly save 5000 yuans, bring certain economic benefit, and methane flash steam gas does not enter in air, environment is not had any impact, there is certain environmental benefit.
Claims (6)
1. use a method for the device process methyl alcohol flash steam of process methyl alcohol flash steam, it is characterized in that a kind of method of the device process methyl alcohol flash steam of process methyl alcohol flash steam that uses specifically completes according to the following steps:
One, adjusting gas flow: first open the first valve (2), the second valve (3) and the 3rd valve (4), regulate the first valve (2), the gas flow making the purification coal gas containing 12% ~ 18% methane gas enter into heat exchanger tube (5-1) from purified gas inlet tube (1) by the first valve (2) is 111800Nm
3/ h; Regulate the second valve (3), the gas flow making the purification coal gas containing 12% ~ 18% methane gas enter into fuel gas surge tank (6) from purified gas inlet tube (1) by the second valve (3) is 1130Nm
3/ h; Regulate the 3rd valve (4), the gas flow making the gas in fuel gas surge tank (6) enter into flame distributor (5-2) is 2240m
3/ h;
Two, reforming gas is prepared in reaction: flame distributor (5-2) naked light burns the gas entered from fuel gas surge tank (6), by the purification heated by gas in heat exchanger tube (5-1), being warming up to 550 DEG C, is then that the purification coal gas of 550 DEG C enters into converter (8) by temperature; Oxygen and water vapour are entered into converter (8) from oxygen and water vapour inlet pipe (7), temperature is the purification coal gas of 550 DEG C and the oxygen entered from oxygen and water vapour inlet pipe (7) and the combustion chamber mixed firing of water vapour on converter (8) top, and then the beds through converter (8) bottom, carry out the steam reforming reaction of hydro carbons, obtain the reforming gas that temperature is 1002 DEG C;
Three, methanol-fueled CLC reaction: temperature is that the reforming gas of 1002 DEG C enters into Heat Exchanger in Circulating Water System (16) cooling, temperature drops to 40 DEG C, then compressor (9) is entered into, the pressure of reforming gas is risen to 8.3MPa by compressor (9), then inlet tower gas interchanger (17) is entered into, temperature rises to 225 DEG C, the adiabatic catalytic oxidant layer of synthetic tower (10) interior tubulation is entered into again from synthetic tower (10) top, flow through tubulation inner catalyst bed after intensification from top to bottom and carry out methanol-fueled CLC reaction, obtain reaction gas;
Four, cool, be separated: reaction gas from synthetic tower (10) bottom out, enter into water cooler (11) and be cooled to 40 DEG C, crude carbinol is isolated again from water cooler (11), crude carbinol is discharged from the bottom of methyl alcohol water cooler (11), enters into flash drum (12); Reforming gas in water cooler (11) from the exit end at the top of water cooler (11) out, enters into compressor (9), re-starts building-up reactions; The crude carbinol entering into flash drum (12) discharges methyl alcohol flash steam through flash drum (12) decompression, methyl alcohol flash steam is discharged from the upper end of flash drum (12), enter into flash steam separator (14), again after flash steam separator (14) is separated, discharge from the upper end of flash steam separator (14), enter into fuel gas surge tank (6); The methyl alcohol separated through flash drum (12) and flash steam separator (14) enters into methanol outlet pipe (15), discharges, the method for the process methyl alcohol flash steam namely completed through methanol outlet pipe (15);
A kind of device processing methyl alcohol flash steam comprises purified gas inlet tube (1), first valve (2), second valve (3), 3rd valve (4), process furnace (5), fuel gas surge tank (6), oxygen and water vapour inlet pipe (7), converter (8), compressor (9), synthetic tower (10), water cooler (11), flash drum (12), exhaust-valve (13), flash steam separator (14), methanol outlet pipe (15), Heat Exchanger in Circulating Water System (16) and inlet tower gas interchanger (17),
Heat exchanger tube (5-1) and flame distributor (5-2) is provided with in described process furnace (5); Described purified gas inlet tube (1) is connected with the inlet end of fuel gas surge tank (6) with the inlet end of heat exchanger tube (5-1) respectively; Be provided with the first valve (2) between purified gas inlet tube (1) and heat exchanger tube (5-1), between purified gas inlet tube (1) and fuel gas surge tank (6), be provided with the second valve (3); The exit end of fuel gas surge tank (6) is connected with flame distributor (5-2), and is provided with the 3rd valve (4) between fuel gas surge tank (6) and flame distributor (5-2); The exit end of heat exchanger tube (5-1) is connected with the entrance end of converter (8) with water vapour inlet pipe (7) inlet end respectively with oxygen; The exit end of converter (8) is connected with the inlet end of Heat Exchanger in Circulating Water System (16), and the exit end of Heat Exchanger in Circulating Water System (16) is connected with the inlet end of compressor (9); The exit end of compressor (9) is connected with the inlet end of inlet tower gas interchanger (17), the exit end of inlet tower gas interchanger (17) is connected with the inlet end of synthetic tower (10), and the exit end of synthetic tower (10) is connected with the inlet end of water cooler (11); The exit end of water cooler (11) is connected with the inlet end of flash drum (12); The top exit end of flash drum (12) is connected with the inlet end of flash steam separator (14); The top exit end of flash steam separator (14) is connected with fuel gas surge tank (6); The outlet at bottom end of flash drum (12) is connected with methanol outlet pipe (15) respectively with the outlet at bottom end of flash steam separator (14);
The exit end at described water cooler (11) top is connected with the inlet end at compressor (9) top;
Exhaust-valve (13) is provided with between described flash drum (12) and flash steam separator (14);
Be provided with tubulation in described synthetic tower (10), tubulation is built with catalyzer.
2. a kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam according to claim 1, is characterized in that temperature in step 2 is that the contents on dry basis of methane in the reforming gas of 1002 DEG C is less than 0.5%.
3. a kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam according to claim 1, is characterized in that temperature in step 2 be the composition of the reforming gas of 1002 DEG C is CO
2, CO, H
2and H
2o.
4. a kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam according to claim 1, is characterized in that the main component of the methyl alcohol flash steam described in step 4 is carbonic acid gas, carbon monoxide, methane, ethane, hydrogen, nitrogen, first alcohol and water; Wherein the content of carbonic acid gas is 11.7% ~ 12.5%, the content of carbon monoxide is 3.7% ~ 4.6%, the content of methane is 38.3% ~ 40.5%, the content of ethane is 2.4% ~ 3.6%, the content of hydrogen is 33.8% ~ 38.3%, the content of nitrogen is 0.7% ~ 0.8%, and the content of methyl alcohol is 6.3% ~ 7.2%, and the content of water is 0.18%.
5. a kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam according to claim 1, it is characterized in that in step 4, methyl alcohol flash steam is discharged from the upper end of flash steam separator (14), the gas flow entering into fuel gas surge tank (6) is 2000m
3/ h.
6. a kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam according to claim 1, is characterized in that the reaction gas in step 3 is CH
3oH and H
2o.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410675418.2A CN104387230B (en) | 2014-11-21 | 2014-11-21 | A kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410675418.2A CN104387230B (en) | 2014-11-21 | 2014-11-21 | A kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104387230A CN104387230A (en) | 2015-03-04 |
| CN104387230B true CN104387230B (en) | 2016-02-10 |
Family
ID=52605209
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410675418.2A Expired - Fee Related CN104387230B (en) | 2014-11-21 | 2014-11-21 | A kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104387230B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105175223B (en) * | 2015-08-31 | 2017-03-15 | 四川天一科技股份有限公司 | Methanol synthesis reaction gas is used for methanol pre-rectifying tower heating system |
| CN105439086B (en) * | 2016-01-26 | 2017-06-16 | 中煤能源黑龙江煤化工有限公司 | A kind of nitrogen for part oxidizing system is without circulation heat riser |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4968722A (en) * | 1988-02-05 | 1990-11-06 | Process Engineering Consultants Pec B.V. | Process for producing methanol |
| US6100303A (en) * | 1997-11-27 | 2000-08-08 | Toyo Engineering Corporation | Method of producing methanol |
| CN101302139A (en) * | 2008-07-07 | 2008-11-12 | 西南化工研究设计院 | Method for preparing methanol using coal bed gas |
| CN101429098A (en) * | 2008-12-03 | 2009-05-13 | 西南化工研究设计院 | Method for synthesis of methanol with CO, CO2 and H#[-2] |
| CN202509006U (en) * | 2012-03-19 | 2012-10-31 | 四川天一科技股份有限公司 | Device for producing methanol by using methanol exhausted gas |
| CN203007175U (en) * | 2012-12-19 | 2013-06-19 | 新奥科技发展有限公司 | Heat integration device for methanol synthesis and rectification |
| CN203095912U (en) * | 2012-12-28 | 2013-07-31 | 中石化宁波工程有限公司 | Methanol synthesis system |
| CN204237725U (en) * | 2014-11-21 | 2015-04-01 | 中煤能源黑龙江煤化工有限公司 | A kind of device processing methyl alcohol flash steam |
-
2014
- 2014-11-21 CN CN201410675418.2A patent/CN104387230B/en not_active Expired - Fee Related
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4968722A (en) * | 1988-02-05 | 1990-11-06 | Process Engineering Consultants Pec B.V. | Process for producing methanol |
| US6100303A (en) * | 1997-11-27 | 2000-08-08 | Toyo Engineering Corporation | Method of producing methanol |
| CN101302139A (en) * | 2008-07-07 | 2008-11-12 | 西南化工研究设计院 | Method for preparing methanol using coal bed gas |
| CN101429098A (en) * | 2008-12-03 | 2009-05-13 | 西南化工研究设计院 | Method for synthesis of methanol with CO, CO2 and H#[-2] |
| CN202509006U (en) * | 2012-03-19 | 2012-10-31 | 四川天一科技股份有限公司 | Device for producing methanol by using methanol exhausted gas |
| CN203007175U (en) * | 2012-12-19 | 2013-06-19 | 新奥科技发展有限公司 | Heat integration device for methanol synthesis and rectification |
| CN203095912U (en) * | 2012-12-28 | 2013-07-31 | 中石化宁波工程有限公司 | Methanol synthesis system |
| CN204237725U (en) * | 2014-11-21 | 2015-04-01 | 中煤能源黑龙江煤化工有限公司 | A kind of device processing methyl alcohol flash steam |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104387230A (en) | 2015-03-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101208264B (en) | Compact reforming reactor | |
| CN101222975B (en) | Compact reforming reactor | |
| RU2604624C2 (en) | Method and device for gasification of biomass by recycling carbon dioxide without oxygen | |
| CN100500550C (en) | Method of preparing hydrogen by reforming methanol-water steam | |
| CN103242134A (en) | Pyrolysis gasification and purification method of household garbage | |
| CN101973523B (en) | Method for preparing hydrogen gas by taking marsh gas as raw material | |
| CN102381717B (en) | Method for converting natural gas to produce ammonia | |
| CN109181776B (en) | Coal-based poly-generation system and method for integrated fuel cell power generation | |
| CN102942972A (en) | Method for producing liquefied natural gas by coke oven gas | |
| CN101993730B (en) | Multifunctional energy system based on appropriate conversion of chemical energy of fossil fuel | |
| Moneti et al. | Simulations of a plant with a fluidized bed gasifier WGS and PSA | |
| CN101302139B (en) | Method for preparing methanol using coal bed gas | |
| CN101148250B (en) | Joint production process of alcohol and ammonia | |
| CN104387230B (en) | A kind of method using the device process methyl alcohol flash steam of process methyl alcohol flash steam | |
| CN103204469B (en) | Full-low-transformation technique for tail gas of calcium carbide furnaces | |
| CN102732317A (en) | Technological process for preparing synthetic gas by using biomass | |
| CN108557764A (en) | A kind of anhydrous process for making hydrogen | |
| CN103421561A (en) | Synthesis gas methanation reaction method | |
| CN204237725U (en) | A kind of device processing methyl alcohol flash steam | |
| CN103524300B (en) | Method for jointly producing methyl alcohol by using water gas and coke oven gas | |
| CN113955718B (en) | Direct reforming process and system for non-catalytic partial oxidation of high-temperature raw gas | |
| RU2515477C2 (en) | Method of obtaining hydrogen | |
| CN102477324A (en) | Method for preparing synthetic natural gas from coal carbonization gas as raw material | |
| RU2587736C1 (en) | Plant for utilisation of low-pressure natural and associated oil gases and method for use thereof | |
| CN103449364A (en) | High-concentration CO sulfur tolerance shift technology and device fully using reaction heat |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160210 Termination date: 20171121 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |