CN107721819A - A kind of method for reducing synthesising gas systeming carbinol system energy consumption and water consume and the system that methanol is prepared by synthesis gas - Google Patents
A kind of method for reducing synthesising gas systeming carbinol system energy consumption and water consume and the system that methanol is prepared by synthesis gas Download PDFInfo
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- CN107721819A CN107721819A CN201610665653.0A CN201610665653A CN107721819A CN 107721819 A CN107721819 A CN 107721819A CN 201610665653 A CN201610665653 A CN 201610665653A CN 107721819 A CN107721819 A CN 107721819A
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- 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
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
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- C—CHEMISTRY; METALLURGY
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- 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
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Abstract
The present invention relates to industry methanol field, discloses a kind of method for reducing synthesising gas systeming carbinol system energy consumption and water consume and the system that methanol is prepared by synthesis gas.Methods described includes being reacted raw material of synthetic gas and obtaining the reaction product containing methanol, reaction product is once cooled down successively, secondary cooling and gas-liquid separation, the liquid product that gas-liquid separation is obtained is flashed, and the gas-phase product after flash distillation is condensed, and the mode once cooled down is：The liquid product isolated with raw material of synthetic gas and gas-liquid is exchanged heat reaction product respectively；The gas-phase product that the cooling medium of condensation is obtained by gas-liquid separation provides.The system includes reactor, a cooling unit, secondary cooling unit, gas-liquid separator, flash column and the condenser being sequentially connected, cooling unit includes the first and second heat exchangers, and the gas-phase product outlet of the gas-liquid separator is connected with the cooling medium entrance of the condenser.The present invention can save steam and circulation water consumption.
Description
Technical field
The present invention relates to commercial syngas methanol field, in particular it relates to a kind of synthesising gas systeming carbinol system that reduces
The method of energy consumption and the system that methanol is prepared by synthesis gas.
Background technology
Industrial methanol is in certain temperature, pressure and catalyst by the synthesis gas containing carbon monoxide, carbon dioxide and hydrogen
In the presence of react, reaction product obtains, existing methanol system through steps such as cooling, gas-liquid separation, filtration washing and rectifying
Although standby technique has also carried out appropriate recovery to reaction heat, for large-scale methanol synthesizer, cooling and rectifying
Energy consumption and water consume is still larger (stills need after reactor outlet preheating inlet gas to consume substantial amounts of electric energy and (account for device always to consume energy
30%), while in flash distillation, often producing one ton of methanol needs to consume about 0.15t steam, it is necessary to further reduce, to flash distillation
The circulation water consumption that gas afterwards is condensed is also big.
The content of the invention
The purpose of the present invention is the defects of overcoming energy consumption in the prior art and larger water consume, there is provided one kind can improve system
Efficiency and the method and system that methanol is prepared by synthesis gas for reducing water consume.
To achieve these goals, the invention provides a kind of side for reducing synthesising gas systeming carbinol system energy consumption and water consume
Method, this method include：Reacted raw material of synthetic gas and obtain the reaction product containing methanol, reaction product is carried out successively
Once cooling, secondary cooling and gas-liquid separation, then the liquid product that reaction product gas-liquid separation is obtained are flashed, and will be dodged
Gas-phase product after steaming is condensed, wherein, the mode once cooled down is：It is former with synthesis gas respectively that reaction product is divided into two parts
The liquid product that material and reaction product gas-liquid separation obtain is exchanged heat, so that raw material of synthetic gas and reaction product gas-liquid separation obtain
The temperature of the liquid product arrived raises and the temperature of reaction product reduces；The cooling medium that gas-phase product condensation after flash distillation uses
The gas-phase product partly or entirely obtained by reaction product gas-liquid separation provides.
Invention further provides a kind of system that methanol is prepared by synthesis gas, the system includes the reaction being sequentially connected
Device, a cooling unit, secondary cooling unit, gas-liquid separator, flash column and condenser, wherein, a cooling unit
The liquid phase sent out respectively with the material and gas-liquid separator for entering reactor including the reaction product for reactor to be sent out is produced
The First Heat Exchanger and the second heat exchanger that thing is exchanged heat, gas-phase product outlet and the condenser of the gas-liquid separator
Cooling medium entrance is connected, wherein, reaction product is divided into two parts and produced respectively with the liquid phase of raw material of synthetic gas and gas-liquid separator
Thing is exchanged heat, so that the temperature of the liquid product of raw material of synthetic gas and gas-liquid separator raises and the temperature of reaction product drop
It is low；The cooling medium that condenser uses partly or entirely is provided by the gas-phase product of gas-liquid separator.
Pass through above-mentioned technical proposal, the present invention have recycled synthesising gas systeming carbinol reaction liberated heat and used it for
The workshop section's (i.e. isolated liquid product of raw material of synthetic gas and gas-liquid) heated is needed, so as to effective recycling system
From heat production, the present invention is in addition to saving raw material of synthetic gas and heating the energy consumption used, it is necessary to the temperature of the reactor outlet gas of cooling
Due to being exchanged heat with the liquid product of raw material of synthetic gas and gas-liquid separator, its temperature further reduces degree, reduces two
The load and intensity of secondary cooling (including air cooling and water cooling), thereby saving power consumption or water consume that secondary cooling uses；In addition, this
Invention also by the use of reaction product gas-liquid separation gas-phase product as condenser cooling medium, to from flash column eject come gas
Phase product is condensed, and partly or entirely replaces reduce further system as the cooling medium of condenser generally by the use of water
Water consume.Therefore, method of the invention or system can save steam and circulation water consumption, and reduce energy consumption, be improved so as to overall
System energy efficiency.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is the structural representation according to the system of one embodiment of the present invention.
Embodiment
The embodiment of the present invention is described in detail below.It is it should be appreciated that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The end points of disclosed scope and any value are not limited to the accurate scope or value herein, these scopes or
Value should be understood to comprising the value close to these scopes or value.For number range, between the endpoint value of each scope, respectively
It can be combined with each other between the endpoint value of individual scope and single point value, and individually between point value and obtain one or more
New number range, these number ranges should be considered as specific open herein.
The synthesising gas systeming carbinol system energy consumption and the method for water consume provided by the invention of reducing includes：Carry out raw material of synthetic gas
Reaction obtains the reaction product containing methanol, reaction product is once cooled down successively, secondary cooling and gas-liquid separation, then will
The liquid product that reaction product gas-liquid separation obtains is flashed, and the gas-phase product after flash distillation is condensed, wherein, once
The mode of cooling is：Reaction product is divided into the liquid phase production that two parts obtain with raw material of synthetic gas and reaction product gas-liquid separation respectively
Thing is exchanged heat, so that the temperature for the liquid product that raw material of synthetic gas and reaction product gas-liquid separation obtain raises and reaction product
Temperature reduce；The cooling medium that gas-phase product condensation after flash distillation uses partly or entirely is obtained by reaction product gas-liquid separation
Gas-phase product provide.
In the present invention, the temperature of reaction product is usually 280-290 DEG C, and the mode that reaction product is once cooled down is to change
Heat, the temperature of reaction product is (if reaction product is divided into some and entered respectively from different materials after a cooling heat transferring
Row heat exchange, then the temperature refer to heat exchange after each several part reaction product remix after temperature) at least reduce 130-160 DEG C (as reduce
190-200℃).Methanol synthesis reaction liberated heat can effectively be reclaimed by, which once being cooled down by way of heat exchange, mitigates two
The intensity and load of secondary cooling, so as to save system energy consumption and water consume.Reaction product after heat exchange enters secondary cooling step.
In the preferred embodiment of the present invention, the mode once cooled down is：A part of reaction product and 70-80 DEG C of synthesis
Gas raw material is exchanged heat, and the temperature of raw material of synthetic gas is increased to react required temperature, another part reaction product with
The liquid product of reaction product gas-liquid separation is exchanged heat, and makes the temperature rise for the liquid product that reaction product gas-liquid separation obtains
To 155-165 DEG C, two parts reaction product is mixed again after heat exchange, and mixed temperature is 90-100 DEG C.
Wherein, usually, the raw material of synthetic gas reacted is former by fresh synthesis gas raw material and the synthesis gas of system circulation
Material is mixed to get.Fresh synthesis gas material temperature is usually 140-160 DEG C, and the temperature of the raw material of synthetic gas of system circulation is usually
40-55℃。
It it is preferably 233-237 DEG C into the raw material of synthetic gas temperature in reactor in the present invention.Reaction pressure is preferably 7-
8MPa.Reaction temperature is usually 275-285 DEG C.
In the present invention, the mode of secondary cooling is had no particular limits, as long as reaction product can be reduced further
Temperature causes the temperature of reaction product to be reduced to the temperature (such as 40-55 DEG C) particularly suitable for carrying out gas-liquid separation, for example,
Secondary cooling can be carried out by the way of air cooling and/or water cooling.
Under preferable case, when the temperature of reaction product is 90-100 DEG C afterwards for heat exchange (once cooling down), the side of secondary cooling
Formula is progress air cooling and water cooling successively.Wherein, air cooling can cause the temperature of reaction product to be reduced to 60-70 DEG C, to air cooling
Concrete operations do not require particularly, can implement by air cooler.Water cooling can cause the temperature of reaction product further to drop
As little as 40-55 DEG C, the concrete operations to water cooling do not require particularly, can implement by water cooler.
In the present invention, the condition of reaction product gas-liquid separation is not required particularly, it is for instance possible to use high-pressure gas-liquid
Separation, it is preferred that the condition of gas-liquid separation including temperature is 40-55 DEG C, pressure 7.2-7.9MPa.It is highly preferred that gas
It is 40-45 DEG C that the condition of liquid separation, which includes temperature, on the one hand methanol can be use up within the range by controlling the temperature of gas-liquid separation
May more than condensing out, can also further reduce in addition flash distillation overhead condensation quantity of circulating water (cooling medium substantially may be used
There is provided with the gas-phase product all obtained by the reaction product gas-liquid separation that temperature is preferably 40-45 DEG C).Usually, existing
In technology, gas-phase product that reaction product gas-liquid separation obtains (predominantly unreacted synthesis gas) a part of (can be with compressed)
Raw material of synthetic gas is recycled as (it is generally necessary to be mixed with a certain amount of fresh synthesis gas raw material, to reduce indifferent gas in circulating air
The partial pressure of body, ensure the C/Hratio of raw material of synthetic gas reacted), a part removes hydrogen retrieval as periodic off-gases.
But the gas-phase product (predominantly unreacted synthesis gas) that in the present invention, these reaction product gas-liquid separations obtain
Before it be used to circulate synthesis gas, the cooling medium that is at least partially or fully used as in the condenser that is connected with flash column,
As this partial gas phase product temperatur rise after condenser cooling medium, then it is pressurized or with being not used as the part of cooling medium
Mixed after mixing through pressurization with fresh synthesis gas raw material and be used as raw material of synthetic gas.
In the present invention, flash conditions are not required particularly, for example, flash conditions include：Temperature is 93-96 DEG C, pressure
Power is 0.25-0.35MPa.When using high-pressure gas-liquid separation, the liquid product pressure that gas-liquid separation obtains is higher, before flash distillation
Decompression operation is first carried out to liquid product, so that material is in the pressure for being more suitable for being flashed.Therefore in order to more effectively
Flashed, methods described further comprises that the liquid product that obtains gas-liquid separation is depressurized before flash distillation (can be by subtracting
Pressure valve is carried out) the step of.So that the pressure for the liquid product that gas-liquid separation obtains is reduced to 0.25-0.35MPa, (temperature is about for decompression
For 93-96 DEG C).The mode of operation flashed again after decompression is particularly conducive to remove impurity (such as H in the material containing methanol2、
CO2, CO and CH4Deng).By heat exchange, without provide extra steam again during flash distillation.
In the present invention, the liquid phase that flashes to obtain is methanol product, gas phase can further condensed processing, the liquid of condensation
Body is returned as phegma and flashed, and the gas phase discharged after condensation can use as fuel gas.As it was previously stated, the cooling that condensation uses
Gas-phase product (the i.e. cooling medium, partly or entirely by reaction product gas-liquid point that medium is obtained using reaction product gas-liquid separation
There is provided from obtained gas-phase product).
Therefore, the present invention by the use of reaction product gas-liquid separation gas-phase product as condenser cooling medium, to from sudden strain of a muscle
Steam the gas-phase product that tower top comes out to be condensed, partly or entirely replace generally by the use of water as the cooling medium of condenser, thus
It reduce further the water consume of system.
In the present invention, the raw material of synthetic gas can be the conjunction of conventional use of hydrogen, carbon monoxide and carbon dioxide
Into gas, for example, the mol ratio of three can be (25-30)：(10-12)：1.C/Hratio (H2-CO2)/(CO+CO2) can be
2.05-2.15 (mol ratio).In addition, the reaction is carried out in the presence of a catalyst, the catalyst can be each of routine
Kind catalyst, those skilled in the art can be selected it, such as copper-based catalysts (Cu/Zn/Al2O3), it is no longer superfluous herein
State.
As shown in figure 1, the system provided by the invention that methanol is prepared by synthesis gas includes：The reactor 1, one being sequentially connected
Secondary cooling unit, secondary cooling unit, gas-liquid separator 4, flash column 5 and condenser 7, wherein, a cooling unit bag
Include：The reaction product that reactor 1 is exported is entered with entering the material of reactor and the liquid product of the bottom of gas-liquid separator 4 respectively
The First Heat Exchanger 2a and the second heat exchanger 2b of row heat exchange, gas-phase product outlet and the condenser 7 of the gas-liquid separator 4
Cooling medium entrance be connected (so as to which the gas-phase product of gas-liquid separator 4 is introduced into described condenser 7 as cooling medium).Its
In, " being sequentially connected " refers to that the material outlet of previous unit is connected with the material inlet of next unit, such as the thing of gas-liquid separator 4
Material outlet is connected with the material inlet of flash column 5.
Wherein, reaction product is divided into liquid product of the two parts respectively with raw material of synthetic gas and gas-liquid separator 4 and changed
Heat, so that the temperature of the liquid product of raw material of synthetic gas and gas-liquid separator 4 raises and the reduction of the temperature of reaction product；Condenser
7 cooling mediums used are partly or entirely provided by the gas-phase product of gas-liquid separator 4.
According to the preferred embodiment of the present invention, the secondary cooling unit includes air cooler 3a and the water cooling being sequentially connected
Device 3b.The second heat exchanger 2b is preferably high pressure heat exchanger.
According to the preferred embodiment of the present invention, the gas-liquid separator can be high-pressure gas-liquid separator.Usually, from
The gas-phase product part discharged in gas-liquid separator is recycled as raw material of synthetic gas (can be compressed through recycle gas compressor 8),
A part removes hydrogen retrieval as periodic off-gases, and therefore, the system can also include being used for the gas that will be discharged from gas-liquid separator
Phase product section is recycled to the pipeline of reactor and the recycle gas compressor 8 for compressed recycle gas.Used in the condenser 7
Cooling medium partly or entirely provided by the gas-phase product discharged in gas-liquid separator, and be used for condensed gas-phase product temperature
Degree rise, can be recycled to mix with fresh synthesis gas raw material and be used as raw material of synthetic gas, therefore, the gas-phase product in condenser 7
It is recyclable to be used as raw material of synthetic gas.
According to the present invention, in order to be more effectively carried out flashing, so as to more effectively remove the impurity in material, the system
It may further include the pressure-reducing valve 6 being arranged between gas-liquid separator and flash column and (specifically, be arranged on the second heat exchanger 2b
Downstream, i.e., between the second heat exchanger 2b and flash column 5), for reduce gas-liquid separator submitting liquid product pressure.
According to the present invention, the system includes being used to condense the condenser 7 of the gas of flash column submitting.Methanol product is from sudden strain of a muscle
The outlet at bottom discharge of tower is steamed, the gas at the top of flash column is used as fuel gas after being condensed with condensed device 7, and the liquid of condensation
Flash column is returned as phegma.
According to the present invention it is possible to heat is taken to produce steam in being obtained from reactor by way of tubulation is set, for it
Its purposes.
The application method of system of the present invention can be：Raw material of synthetic gas is set to be reacted and be contained in reactor 1
There is the reaction product of methanol, reaction product is introduced to a cooling unit, secondary cooling unit (such as air cooler 3a and water cooling successively
Device 3b) and gas-liquid separator 4, then the liquid product discharged in gas-liquid separator is depressurized by pressure-reducing valve 6, then will decompression
Material afterwards introduces flash column 5 and flashed, and the condensed device 7 of gas of flash distillation column overhead discharge condenses (to be arranged in gas-liquid separator
The gas-phase product gone out, which is directed in condenser, is used as cooling medium), the liquid of condensation returns to flash column, condenser as phegma
The gas of discharge can be used as fuel gas, wherein, part or all of reaction product is exchanged heat by First Heat Exchanger 2a and second respectively
Device 2b is exchanged heat with raw material of synthetic gas and liquid product, so that the temperature of raw material of synthetic gas and liquid product raises and reacts production
The temperature of thing reduces.
The method or system of the present invention prepares MTO level methanol particularly suitable for synthesis gas, in order to which methanol is further purified, this
The step of method or system of invention may further include purifying or unit, are no longer repeated one by one herein.
The present invention will be described in detail by way of examples below.In following examples, raw material of synthetic gas is hydrogen, one
The mixed gas of carbonoxide and carbon dioxide, wherein, the mol ratio of hydrogen, carbon monoxide and carbon dioxide is 27:11:1；Reaction
The volume of device is 280m3(annual production of methanol is about 1,200,000 tons)；Catalyst is Cu/Zn/Al2O3, purchased from Britain
JohnsonMamley companies, article No. KATALCOJM51-9,200 tons of methanol is often produced, the dosage of catalyst is 1 ton.
Embodiment 1
Technical process as shown in figure 1, wherein,
(1) react：Raw material of synthetic gas is preheated into (heat exchange) to 234 DEG C and is continuously passed through reactor according to 167t/h flow
In reacted in the presence of a catalyst, reaction pressure 7.6MPa；
(2) once cool down：The reaction product (285 DEG C) for obtaining step (1) by heat exchanger is exchanged heat；
(3) secondary cooling：Reaction product after cooling heat transferring is cooled to 65 DEG C, then water cooled device drop through air cooler
Temperature is to 53 DEG C；
(4) gas-liquid separation：Product after secondary cooling, which enters, carries out gas-liquid separation (7.7MPa) in gas-liquid separator, obtain
Liquid product and gas-phase product；
(5) depressurize：Liquid product is depressurized to 0.32MPa through pressure-reducing valve；
(6) flash：Material after decompression is passed through into flash column to be flashed, the temperature of charge for entering flash column is 94 DEG C, tower
It is 50 DEG C, pressure 0.27MPa to push up temperature, and bottom of towe is MTO levels methanol (content of methanol is 95 weight %), and temperature is 96 DEG C, with
150t/h flow draws flash column；
(7) condense：The gas-phase product (53 DEG C) that gas-liquid separation is obtained is as part cooling medium (while by partly following
Ring water) gas (89 DEG C) that goes out to flash column top row condenses, and (50 DEG C) of liquid under condensing returns to flash distillation as phegma,
The gas phase discharged after condensation uses as fuel gas；
Wherein, the mode of a cooling heat transferring is：Partial reaction product (the 84.8 weight % for accounting for overall reaction product) and temperature
The raw material of synthetic gas spent for 77 DEG C exchanged heat (BEM type heat exchangers, similarly hereinafter) to be passed through raw material of synthetic gas in reactor
Temperature rise is 234 DEG C and the temperature of the partial reaction product is reduced to 95 DEG C, and another part reaction product (accounts for overall reaction product
15.2 weight %) with the liquid product of gas-liquid separation exchanged heat (BEM type high pressure heat exchangers, similarly hereinafter) cause gas-liquid separation
The temperature rise of liquid product is 163 DEG C and the temperature of the partial reaction product is reduced to 62 DEG C, two parts reaction after heat exchange
(temperature is 91 DEG C) enters secondary cooling after product mixing.
In the technique, dosage (being calculated by Aspen Plus, similarly hereinafter), the system of 0.46MPa Preheated steams use
Quantity of circulating water and unit efficiency (reference standard GBT2589-2008 is calculated, similarly hereinafter) are as shown in table 1 respectively.
Embodiment 2
Technical process as shown in figure 1, wherein,
(1) react：Raw material of synthetic gas is heated into (heat exchange) to 233 DEG C and is continuously passed through reactor according to 167t/h flow
In reacted in the presence of a catalyst, reaction pressure 8MPa；
(2) once cool down：The reaction product (284 DEG C) for obtaining step (1) by heat exchanger is exchanged heat；
(3) secondary cooling：Reaction product after cooling heat transferring is cooled to 60 DEG C, then water cooled device drop through air cooler
Temperature is to 45 DEG C；
(4) gas-liquid separation：Product after secondary cooling, which enters, carries out gas-liquid separation (7.2MPa) in gas-liquid separator, obtain
Liquid product and gas-phase product；
(5) depressurize：Liquid product is depressurized to 0.35MPa through pressure-reducing valve；
(6) flash：Material after decompression is passed through into flash column to be flashed, the temperature for entering the material of flash column is 93 DEG C,
Tower top temperature is 50 DEG C, pressure 0.3MPa, and bottom of towe is MTO levels methanol (content of methanol is 95 weight %), and temperature is 96 DEG C, with
150t/h flow draws flash column；
(7) condense：The gas that the gas-phase product (45 DEG C) that gas-liquid separation is obtained goes out as cooling medium to flash column top row
Body (89 DEG C) is condensed, and (50 DEG C) of liquid under condensing returns to flash distillation as phegma, and the gas phase discharged after condensation is as combustion
Expect that gas uses；
Wherein, the mode of a cooling heat transferring is：Partial reaction product (the 86 weight % for accounting for overall reaction product) and temperature
Heat exchange is carried out for 70 DEG C of raw material of synthetic gas so that the temperature rise for the raw material of synthetic gas being passed through in reactor is 233 DEG C and the portion
The temperature of point reaction product is reduced to 94 DEG C, another part reaction product (the 14 weight % for accounting for overall reaction product) and gas-liquid separation
Liquid product carry out heat exchange and make it that the temperature rise of the liquid product of gas-liquid separation is 155 DEG C and the temperature of the partial reaction product
Degree is reduced to 64 DEG C, and (temperature is 90 DEG C) enters secondary cooling after two parts reaction product mixing after heat exchange.
In the technique, quantity of circulating water and unit efficiency that dosage, the system of 0.46MPa Preheated steams use are respectively such as table 1
It is shown.
Embodiment 3
Technical process as shown in figure 1, wherein,
(1) react：Raw material of synthetic gas is heated into (heat exchange) to 237 DEG C and is continuously passed through reactor according to 167t/h flow
In reacted in the presence of a catalyst, the pressure of reaction is 7MPa；
(2) once cool down：The reaction product (286 DEG C) for obtaining step (1) by heat exchanger is exchanged heat；
(3) secondary cooling：Reaction product after cooling heat transferring is cooled to 70 DEG C, then water cooled device drop through air cooler
Temperature is to 40 DEG C；
(4) gas-liquid separation：Product after secondary cooling, which enters, carries out gas-liquid separation (7.9MPa) in gas-liquid separator, obtain
Liquid product and gas-phase product；
(5) depressurize：Liquid product is depressurized to 0.3MPa through pressure-reducing valve；
(6) flash：Material after decompression is passed through into flash column to be flashed, the temperature for entering the material of flash column is 96 DEG C,
Tower top (fuel gas) temperature is 50 DEG C, pressure 0.25MPa, and bottom of towe is MTO levels methanol (content of methanol is 95 weight %), temperature
For 96 DEG C, flash column is drawn with 150t/h flow；
(7) condense：The gas that the gas-phase product (40 DEG C) that gas-liquid separation is obtained goes out as cooling medium to flash column top row
Body (89 DEG C) is condensed, and (50 DEG C) of liquid under condensing returns to flash distillation as phegma, and the gas phase discharged after condensation is as combustion
Expect that gas uses；
Wherein, the mode of a cooling heat transferring is：Partial reaction product (the 84 weight % for accounting for overall reaction product) and temperature
Heat exchange is carried out for 80 DEG C of raw material of synthetic gas so that the temperature rise for the raw material of synthetic gas being passed through in reactor is 237 DEG C and the portion
The temperature of point reaction product is reduced to 98 DEG C, another part reaction product (the 16 weight % for accounting for overall reaction product) and gas-liquid separation
Liquid product carry out heat exchange and make it that the temperature rise of the liquid product of gas-liquid separation is 165 DEG C and the temperature of the partial reaction product
Degree is reduced to 61 DEG C, and (temperature is 96 DEG C) enters secondary cooling after two parts reaction product mixing after heat exchange.
In the technique, quantity of circulating water and unit efficiency that dosage, the system of 0.46MPa Preheated steams use are respectively such as table 1
It is shown.
Embodiment 4
Method according to embodiment 1 prepares methanol, unlike：One time cooling heat transferring mode is：Partial reaction product (accounts for
85 weight % of overall reaction product) exchange heat so that being passed through the synthesis gas in reactor for 69 DEG C of raw material of synthetic gas with temperature
The temperature rise of raw material is 234 DEG C and the temperature of the partial reaction product is reduced to 92 DEG C, and another part reaction product (accounts for total anti-
Answer 15 weight % of product) carry out heat exchange with the liquid product of gas-liquid separation the temperature of the liquid product of gas-liquid separation is raised
For 153 DEG C, the temperature of the partial reaction product is reduced to 70 DEG C, after two parts reaction product mixing after a cooling heat transferring
(temperature is 88 DEG C) enters secondary cooling.In the technique, quantity of circulating water that dosage, the system of 0.46MPa Preheated steams use and
Unit energy consumption difference is as shown in table 1.
Comparative example 1
Method according to embodiment 1 prepares methanol, unlike：The mode of cooling heat transferring is：Partial reaction product
(the 95 weight % for accounting for overall reaction product) carry out heat exchange so that being passed through the conjunction in reactor with the raw material of synthetic gas that temperature is 77 DEG C
Into gas raw material temperature rise for 234 DEG C and the temperature of the partial reaction product is reduced to 106 DEG C, by the partial reaction product with
(temperature be 102 DEG C) enters secondary cooling after the mixing of another part reaction product, now, during flash distillation needs additionally to consume
0.46MPa Preheated steam.In the technique, quantity of circulating water and unit energy consumption that dosage, the system of 0.46MPa Preheated steams use
It is as shown in table 1 respectively.
Comparative example 2
Method according to embodiment 1 prepares methanol, unlike：The mode of cooling heat transferring is：Partial reaction product
The liquid product of (the 50 weight % for accounting for overall reaction product) and gas-liquid separation carries out the liquid product that heat exchange causes gas-liquid separation
Temperature rise is 165 DEG C and the temperature of the partial reaction product is reduced to 199 DEG C, and the partial reaction product and another part is anti-
(temperature is 197 DEG C) enters secondary cooling after answering product mixing.In the technique, dosage, the system of 1.7MPa Preheated steams use
Quantity of circulating water and unit energy consumption difference it is as shown in table 1.
Comparative example 3
Method according to embodiment 1 prepares methanol, unlike：The reaction product that step (1) obtains directly carries out secondary
Cool down and flash column top row is gone out as cooling medium without once cooling down, and without using the gas-phase product that gas-liquid separation obtains
Gas condensed, and be all used as cooling medium using recirculated water.In the technique, the dosage of 1.7MPa Preheated steams, it is
Quantity of circulating water and unit the energy consumption difference that system uses are as shown in table 1.
Table 1
| Embodiment is numbered | The dosage (t/h) of Preheated steam | Quantity of circulating water (t/h) | Unit efficiency (%) |
| Embodiment 1 | 0 | 5672 | 76% |
| Embodiment 2 | 0 | 5966 | 75.9% |
| Embodiment 3 | 0 | 5666 | 76% |
| Embodiment 4 | 0 | 6780 | 74.8% |
| Comparative example 1 | 19 | 7550 | 71.5% |
| Comparative example 2 | 134(1.7MPa) | 12000 | 54% |
| Comparative example 3 | 256(1.7MPa) | 12000 | 37% |
As can be seen from the above embodiments, method of the invention or system can effectively improve system energy efficiency and reduce water
Consumption.Especially, embodiment 1 carries out once cooling (exchange heat) according to the preferred embodiment of the present invention, and embodiment 4 not according to
Preferred embodiment is carried out, and the result of comparing embodiment 1 and embodiment 4 can be seen that according to the preferred embodiment of the present invention
System energy efficiency can further be improved by carrying out once cooling；In addition, comparative example 1 is only changed reaction product and raw material of synthetic gas
Heat, and comparative example 2 is only exchanged heat reaction product and the liquid product of gas-liquid separation, comparing embodiment 1 and comparative example 1-2's
As a result as can be seen that system energy efficiency can not be effectively improved by only carrying out part heat exchange.Comparative example 3 is not exchanged heat or using gas-liquid
Gas-phase product caused by separation is as cooling medium, and so as to which energy consumption and quantity of circulating water are significantly higher than embodiment 1, system energy efficiency is low.
The preferred embodiment of the present invention described in detail above, still, the present invention are not limited in above-mentioned embodiment
Detail, in the range of the technology design of the present invention, a variety of simple variants can be carried out to technical scheme, this
A little simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (10)
- A kind of 1. method for reducing synthesising gas systeming carbinol system energy consumption and water consume, it is characterised in that this method includes：Make synthesis gas Raw material is reacted to obtain the reaction product containing methanol, reaction product is once cooled down successively, secondary cooling and gas-liquid Separation, then the liquid product that reaction product gas-liquid separation is obtained are flashed, and the gas-phase product after flash distillation is condensed, Wherein, the mode once cooled down is：Reaction product is divided into two parts and obtained respectively with raw material of synthetic gas and reaction product gas-liquid separation To liquid product exchanged heat so that the liquid product that raw material of synthetic gas and reaction product gas-liquid separation obtain temperature rise And the temperature of reaction product reduces；The cooling medium that gas-phase product condensation after flash distillation uses is partly or entirely by reaction product gas The isolated gas-phase product of liquid provides.
- 2. according to the method for claim 1, wherein, the temperature of the reaction product is 280-290 DEG C；Cooling heat transferring Afterwards, the temperature of reaction product at least reduces 130-160 DEG C.
- 3. method according to claim 1 or 2, wherein, the mode once cooled down is：A part of reaction product and 70-80 DEG C raw material of synthetic gas exchanged heat so that the preheated temperature of raw material of synthetic gas is increased to react required temperature；It is another The liquid product that partial reaction product obtains with reaction product gas-liquid separation is exchanged heat, so that reaction product gas-liquid separation obtains The temperature of liquid product be increased to 155-165 DEG C, above-mentioned two parts reaction product is mixed and mixed so after heat exchange Temperature is 90-100 DEG C.
- 4. according to the method for claim 1, wherein, the temperature into the raw material of synthetic gas in reactor is 233-237 DEG C, Reaction pressure is 7-8MPa, and reaction temperature is 275-285 DEG C.
- 5. according to the method for claim 1, wherein, the liquid phase obtained with raw material of synthetic gas and reaction product gas-liquid separation is produced After thing heat exchange, the temperature of reaction product is 90-100 DEG C, and the mode of secondary cooling is progress air cooling and water cooling successively.
- 6. according to the method for claim 1, wherein, the condition of reaction product gas-liquid separation includes temperature and is 40-55 DEG C, presses Power is 7.2-7.9MPa.
- 7. according to the method for claim 1, wherein, flash conditions include：Temperature is 93-96 DEG C, pressure 0.25- 0.35MPa。
- A kind of 8. system that methanol is prepared by synthesis gas, it is characterised in that the system include be sequentially connected reactor (1), one Secondary cooling unit, secondary cooling unit, gas-liquid separator (4), flash column (5) and condenser (7), wherein, it is described once to cool down Unit includes：By the reaction product of reactor (1) outlet respectively with entering material and gas-liquid separator (4) bottom of reactor The First Heat Exchanger (2a) and the second heat exchanger (2b) that liquid product is exchanged heat, the gas-phase product of the gas-liquid separator (4) Outlet is connected with the cooling medium entrance of the condenser (7),Wherein, reaction product is divided into liquid product of the two parts respectively with raw material of synthetic gas and gas-liquid separator (4) and exchanged heat, So that the temperature of the liquid product of raw material of synthetic gas and gas-liquid separator (4) raises and the reduction of the temperature of reaction product；Condenser (7) cooling medium used is partly or entirely provided by the gas-phase product of gas-liquid separator (4).
- 9. system according to claim 8, wherein, the secondary cooling unit include the air cooler (3a) being sequentially connected and Water cooler (3b).
- 10. system according to claim 8 or claim 9, wherein, second heat exchanger (2b) is high pressure heat exchanger, the system System also includes the pressure-reducing valve (6) for being arranged at the second heat exchanger (2b) downstream.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1144214A (en) * | 1995-08-25 | 1997-03-05 | 中国科学院山西煤炭化学研究所 | Method for synthesizing methyl alcohol |
| CN102433169A (en) * | 2011-08-30 | 2012-05-02 | 中国石油化工股份有限公司 | Low temperature methanol washing technology |
| CN105481646A (en) * | 2014-09-15 | 2016-04-13 | 中国石油天然气股份有限公司 | Methanol synthesis separation refrigeration method |
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2016
- 2016-08-12 CN CN201610665653.0A patent/CN107721819B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1144214A (en) * | 1995-08-25 | 1997-03-05 | 中国科学院山西煤炭化学研究所 | Method for synthesizing methyl alcohol |
| CN102433169A (en) * | 2011-08-30 | 2012-05-02 | 中国石油化工股份有限公司 | Low temperature methanol washing technology |
| CN105481646A (en) * | 2014-09-15 | 2016-04-13 | 中国石油天然气股份有限公司 | Methanol synthesis separation refrigeration method |
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