U.S. patent application number 13/232036 was filed with the patent office on 2013-02-07 for method and device for producing methanol.
The applicant listed for this patent is Wu-Jang Huang, Jr-Ming Miao, Chang-Hsien Tai, Yao-Nan Wang. Invention is credited to Wu-Jang Huang, Jr-Ming Miao, Chang-Hsien Tai, Yao-Nan Wang.
Application Number | 20130032488 13/232036 |
Document ID | / |
Family ID | 47626270 |
Filed Date | 2013-02-07 |
United States Patent
Application |
20130032488 |
Kind Code |
A1 |
Tai; Chang-Hsien ; et
al. |
February 7, 2013 |
Method and Device for Producing Methanol
Abstract
A method for producing methanol includes dissolving carbon
dioxide in water to obtain a two-phase coexistence aqueous solution
that is pressurized and heated to a critical state to separate
critical state carbon dioxide and critical water. The critical
state carbon dioxide is reduced to critical state carbon monoxide.
The critical water is electrolyzed to obtain super critical state
hydrogen and super critical state oxygen. The critical state carbon
monoxide reacts with the super critical state hydrogen to produce
methanol. Furthermore, a device for producing methanol is also
provided in the present invention, comprising a mixing unit, a
conversion unit and a synthesis unit, and which is highly effective
in producing methanol and frugal in energy use.
Inventors: |
Tai; Chang-Hsien; (Neipu
Hsiang, TW) ; Miao; Jr-Ming; (Neipu Hsiang, TW)
; Huang; Wu-Jang; (Neipu Hsiang, TW) ; Wang;
Yao-Nan; (Neipu Hsiang, TW) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
Tai; Chang-Hsien
Miao; Jr-Ming
Huang; Wu-Jang
Wang; Yao-Nan |
Neipu Hsiang
Neipu Hsiang
Neipu Hsiang
Neipu Hsiang |
|
TW
TW
TW
TW |
|
|
Family ID: |
47626270 |
Appl. No.: |
13/232036 |
Filed: |
September 14, 2011 |
Current U.S.
Class: |
205/412 ;
204/274; 204/275.1; 204/277; 204/278 |
Current CPC
Class: |
C25B 3/04 20130101; Y02E
60/366 20130101; C25B 15/08 20130101; C25B 9/00 20130101; Y02E
60/36 20130101; C25B 1/12 20130101 |
Class at
Publication: |
205/412 ;
204/275.1; 204/277; 204/274; 204/278 |
International
Class: |
C25B 3/04 20060101
C25B003/04; C25B 15/00 20060101 C25B015/00; C25B 9/00 20060101
C25B009/00 |
Foreign Application Data
Date |
Code |
Application Number |
Aug 2, 2011 |
TW |
100127416 |
Claims
1. A method for producing methanol comprising: a pre-step including
dissolving carbon dioxide in water to obtain a two-phase
coexistence aqueous solution; a conversion step including:
pressurizing and heating the two-phase coexistence aqueous solution
to a critical state to separate critical state carbon dioxide and
critical water from the two-phase coexistence aqueous solution,
reducing the critical state carbon dioxide to critical state carbon
monoxide, and electrolyzing the critical water to obtain super
critical state hydrogen and super critical state oxygen; and a
synthesis step including reacting the critical state carbon
monoxide with the super critical state hydrogen to produce
methanol.
2. The method for producing methanol as claimed in claim 1, with
the two-phase coexistence aqueous solution in the critical state
having a pressure of 221 atm and a temperature of 672K.
3. The method for producing methanol as claimed in claim 1, with
the two-phase coexistence aqueous solution being pressurized and
heated in the pre-step to turn the two-phase coexistence aqueous
solution with carbon dioxide into a high temperature/high pressure
state.
4. The method for producing methanol as claimed in claim 3, with
the two-phase coexistence aqueous solution in the high
temperature/high pressure state having a pressure of 20 atm and a
temperature higher than 330K.
5. The method for producing methanol as claimed in claim 3, with
the conversion step including a separation step, a reduction step,
and an electrolysis step, with the critical state carbon monoxide
and the super critical state hydrogen being obtained by the
separation step, the reduction step, and the electrolysis step.
6. The method for producing methanol as claimed in claim 5, with
the separation step including separating high temperature/high
pressure gaseous carbon dioxide and high temperature/high pressure
liquid water from the two-phase coexistence aqueous solution.
7. The method for producing methanol as claimed in claim 5, with
the reduction step including reducing the high temperature/high
pressure gaseous carbon dioxide in high temperature/high pressure
gaseous carbon monoxide and then heating and pressurizing the high
temperature/high pressure gaseous carbon monoxide into critical
state carbon monoxide.
8. The method for producing methanol as claimed in claim 7, with
the reduction step including supplying an electric current of 10-20
A to generate the high temperature/high pressure gaseous carbon
monoxide from the high temperature/high pressure carbon dioxide and
then compressing the gaseous carbon monoxide at 30 atm and 400 k
into the critical state carbon monoxide at 221 atm and 672K.
9. The method for producing methanol as claimed in claim 5, with
the electrolysis step including heating and pressurizing the high
temperature/high pressure liquid water to the critical state to
obtain the critical water and electrolyzing the critical water into
the super critical state hydrogen and the super critical state
oxygen.
10. The method for producing methanol as claimed in claim 9, with
the high temperature/high pressure liquid water in the critical
state having a pressure of 221 atm and a temperature of 672, with
the super critical state hydrogen and the super critical state
oxygen having a pressure of 230 atm and a temperature of 700K.
11. A device for producing methanol comprising: a mixing unit; a
conversion unit connected by a first pipe to the mixing unit, with
a first pressurizing member and a first heating member mounted
between the conversion unit and the mixing unit, with the
conversion unit outputting a critical state gas; and a synthesis
unit connected by a second pipe to the conversion unit, with the
second pipe allowing the critical state gas to flow into the
synthesis unit, with a gas outlet pipe connected to the synthesis
unit, with the gas outlet pipe outputting a synthetic gas in the
synthetic unit.
12. The device for producing methanol as claimed in claim 11, with
the conversion unit including a separator, a reducer, and an
electrolyser, with the separator connected to the reducer by a
first branch pipe, with a second branch pipe connected between the
separator and the electrolyser.
13. The device for producing methanol as claimed in claim 12, with
the synthesis unit connected to the reducer and the electrolyser by
first and second gas inlet pipes, respectively.
14. The device for producing methanol as claimed in claim 13,
further comprising: a second pressurizing member and a second
heating member mounted on the second branch pipe; and a third
pressurizing member and a third heating member mounted on the first
gas inlet pipe connected between the reducer and the synthesis
unit.
15. The device for producing methanol as claimed in claim 12, with
the reducer connected to a current supplier, with the current
supplier supplying the reducer with electric current.
16. The device for producing methanol as claimed in claim 12, with
the electrolyser connected to a current supplier, with the current
supplier supplying the electrolyser with electric current.
17. The device for producing methanol as claimed in claim 12, with
the electrolyser connected to a storage tank by a gas conveying
pipe.
18. The device for producing methanol as claimed in claim 17, with
a plurality of heat dissipating members mounted between the
electrolyser and the storage tank.
19. The device for producing methanol as claimed in claim 12, with
the separator further including an auxiliary heating member, with
the auxiliary heating member heating the separator.
Description
BACKGROUND OF THE INVENTION
[0001] 1. Field of the Invention
[0002] The present invention relates to a method and a device for
producing methanol from biomass and, more particularly, to a method
and a device for producing methanol with improved efficiency while
consuming less energy.
[0003] 2. Description of the Related Art
[0004] Conventionally, methanol is produced through chemical
reconstitution, wherein methane is converted into methanol through
use of a catalyst. However, the chemical reconstitution is slow in
reactive efficiency. Thus, the conventional method can not fulfill
the economic need.
[0005] Pursuant to continuing improvement in the converting
techniques for converting bioenergy, the bioenergy conversion has
been widely applied in various processes in the chemistry
industries. Recovery of carbon dioxide emitted by the green house
effect draws great attention. At the present stage, the carbon
dioxide in the environment can be converted into methanol through
burning, thermal chemical conversion, or biochemical conversion,
seeking reduction in the consumed energy for producing methanol
while recovering the environmental pollutant.
[0006] In Taiwan Patent No. 1230195 entitled "METHOD AND DEVICE FOR
PRODUCING METHANOL FROM BIOMASS", a biomass is gasified to generate
a gas for producing methanol. The gas is carbon monoxide. Water is
electrolyzed in a water-electrolyzing device by electricity
obtained from a solar generator or wind generator to generate
hydrogen and oxygen. When the amount of hydrogen is more than two
times of that of the carbon monoxide, the hydrogen obtained from
electrolysis is supplied to the gas, producing methanol in a
methanol synthesis tower.
[0007] Conventionally, carbon monoxide directly reacts with gaseous
hydrogen obtained from water electrolysis to form the methanol.
However, the bond strength between the hydrogen atom and the oxygen
atom of liquid water at normal temperature and normal pressure does
not permit separation of the hydrogen atom from the oxygen atom.
External strong current must be provided to electrolyze liquid
water to obtain gaseous hydrogen and gaseous oxygen, which consumes
considerable energy and requires a long period of time of
electrolysis to release sufficient gaseous hydrogen. Thus, the
yield of gaseous hydrogen is low, because it is obviously limited
to the reaction time of water electrolysis. The production
efficiency and yield of subsequently formed methanol are also
adversely affected.
[0008] Furthermore, during the process of electrolyzing the liquid
water into gaseous hydrogen and gaseous oxygen, only the gaseous
hydrogen is used to react with carbon monoxide to obtain methanol.
Namely, the oxygen is not effectively used, leading to a waste and
failing to meet the goal of recovering energy.
[0009] Thus, a need exists for a method and a device for producing
methanol with improved production efficiency while recovering
energy.
SUMMARY OF THE INVENTION
[0010] An objective of the present invention is to provide a method
for producing methanol by using gaseous hydrogen obtained from
electrolyzing critical state liquid water that consumes less
energy, effectively increasing the electrolyzing efficiency of the
liquid water.
[0011] Another objective of the present invention is to provide a
method for producing methanol for increasing the yield of gaseous
hydrogen, effectively increasing the production efficiency of
methanol.
[0012] A further objective of the present invention is to provide a
device for producing methanol that reduces the energy consumed for
producing the methanol, effective saving energy.
[0013] Still another objective of the present invention is to
provide a device for producing methanol that can recover and store
gaseous oxygen obtained from electrolyzing critical state liquid
water to reuse energy.
[0014] The present invention fulfills the above objectives by
providing, in an aspect, a method for producing methanol includes a
pre-step, a conversion step, and a synthesis step. The pre-step
includes dissolving carbon dioxide in water to obtain a two-phase
coexistence aqueous solution. The conversion step includes:
pressurizing and heating the two-phase coexistence aqueous solution
to a critical state to separate critical state carbon dioxide and
critical water, reducing the critical state carbon dioxide to
critical state carbon monoxide, and electrolyzing the critical
water to obtain super critical state hydrogen and super critical
state oxygen. The synthesis step includes reacting the critical
state carbon monoxide with the super critical state hydrogen to
produce methanol.
[0015] Preferably, the two-phase coexistence aqueous solution in
the critical state has a pressure of 221 atm and a temperature of
672K.
[0016] Preferably, the two-phase coexistence aqueous solution is
pressurized and heated in the pre-step to turn the two-phase
coexistence aqueous solution with carbon dioxide into a high
temperature/high pressure state.
[0017] Preferably, the two-phase coexistence aqueous solution in
the high temperature/high pressure state has a pressure of 20 atm
and a temperature higher than 330K.
[0018] Preferably, the conversion step includes a separation step,
a reduction step, and an electrolysis step. The critical state
carbon monoxide and the super critical state hydrogen are obtained
by the separation step, the reduction step, and the electrolysis
step.
[0019] Preferably, the separation step includes separating high
temperature/high pressure gaseous carbon dioxide and high
temperature/high pressure liquid water from the two-phase
coexistence aqueous solution.
[0020] Preferably, the reduction step includes reducing the high
temperature/high pressure gaseous carbon dioxide in high
temperature/high pressure gaseous carbon monoxide and then heating
and pressurizing the high temperature/high pressure gaseous carbon
monoxide into critical state carbon monoxide.
[0021] Preferably, the reduction step includes supplying an
electric current of 10-20 A to generate the high temperature/high
pressure gaseous carbon monoxide from the high temperature/high
pressure carbon dioxide and then compressing the gaseous carbon
monoxide at 30 atm and 400 k into the critical state carbon
monoxide at 221 atm and 672K.
[0022] Preferably, the electrolysis step includes heating and
pressurizing the high temperature/high pressure liquid water to the
critical state to obtain the critical water and electrolyzing the
critical water into the super critical state hydrogen and the super
critical state oxygen.
[0023] Preferably, the high temperature/high pressure liquid water
in the critical state has a pressure of 221 atm and a temperature
of 672, and the super critical state hydrogen and the super
critical state oxygen have a pressure of 230 atm and a temperature
of 700K.
[0024] In another aspect, a device for producing methanol includes
a mixing unit, a conversion unit, and a synthesis unit. The
conversion unit is connected by a first pipe to the mixing unit. A
first pressurizing member and a first heating member are mounted
between the conversion unit and the mixing unit. The conversion
unit outputs a critical state gas. The synthesis unit is connected
by a second pipe to the conversion unit. The second pipe allows the
critical state gas to flow into the synthesis unit. A gas outlet
pipe is connected to the synthesis unit and outputs a synthetic gas
in the synthetic unit.
[0025] Preferably, the conversion unit includes a separator, a
reducer, and an electrolyser. The separator is connected to the
reducer by a first branch pipe, and a second branch pipe is
connected between the separator and the electrolyser.
[0026] Preferably, the synthesis unit is connected to the reducer
and the electrolyser by first and second gas inlet pipes,
respectively.
[0027] Preferably, a second pressurizing member and a second
heating member are mounted on the second branch pipe, and a third
pressurizing member and a third heating member are mounted on the
first gas inlet pipe connected between the reducer and the
synthesis unit.
[0028] Preferably, the reducer is connected to a current supplier
that supplies the reducer with electric current.
[0029] Preferably, the electrolyser is connected to a current
supplier that supplies the electrolyser with electric current.
[0030] Preferably, the electrolyser is connected to a storage tank
by a gas conveying pipe.
[0031] Preferably, a plurality of heat dissipating members is
mounted between the electrolyser and the storage tank.
[0032] Preferably, the separator further includes an auxiliary
heating member for heating the separator.
[0033] The present invention will become clearer in light of the
following detailed description of illustrative embodiments of this
invention described in connection with the drawings.
BRIEF DESCRIPTION OF THE DRAWINGS
[0034] The illustrative embodiments may best be described by
reference to the accompanying drawings where:
[0035] FIG. 1 shows a flowchart illustrating a method for producing
methanol according to the present invention.
[0036] FIG. 2 shows a flowchart illustrating a preferred embodiment
of the method for producing methanol according to the present
invention.
[0037] FIG. 3 shows a schematic diagram of a device for producing
methanol of an embodiment according to the present invention.
[0038] FIG. 4 shows a schematic diagram of a device for producing
methanol of another embodiment according to the present
invention.
[0039] All figures are drawn for ease of explanation of the basic
teachings of the present invention only; the extensions of the
figures with respect to number, position, relationship, and
dimensions of the parts to form the preferred embodiments will be
explained or will be within the skill of the art after the
following teachings of the present invention have been read and
understood. Further, the exact dimensions and dimensional
proportions to conform to specific force, weight, strength, and
similar requirements will likewise be within the skill of the art
after the following teachings of the present invention have been
read and understood.
DETAILED DESCRIPTION OF THE INVENTION
[0040] With reference to FIG. 1, a method for producing methanol
according to the present invention includes a pre-step S1, a
conversion step S2, and a synthesis step S3.
[0041] In the pre-step S1, carbon dioxide in the environment
dissolves in water to obtain two-phase coexistence aqueous solution
with carbon dioxide. The two-phase coexistence aqueous solution is
heated and pressurized to the critical state in the conversion step
S2, obtaining critical state carbon dioxide and critical water. The
critical state carbon dioxide is reduced to critical carbon
monoxide. The critical water is electrolyzed to obtain super
critical state hydrogen and super critical state oxygen. In the
synthesis step S3, the critical state carbon monoxide reacts with
the super critical state hydrogen to obtain methanol. Since the
aqueous solution can be rapidly heated and pressurized, when the
two-phase coexistence aqueous solution reaches the critical state,
gaseous hydrogen can be obtained by critical state water
electrolysis that consumes less energy. The electrolysis efficiency
of liquid water is effectively increased to increase the production
efficiency and yield of methanol.
[0042] By use of the two-phase coexistence aqueous solution that
can rapidly reach the critical state, the present invention can
obtain super critical state hydrogen and super critical state
oxygen from water electrolysis that consumes less energy. To
achieve better effect of less energy consumption, the present
invention uses multiple-stage heating and pressurization which will
is described hereinafter. It can be appreciated by one skilled in
the art that the embodiment is illustrative rather than
restrictive.
[0043] FIG. 2 shows a preferred embodiment of the method for
producing methanol according to the present invention.
Specifically, the method for producing methanol includes a pre-step
S1, a conversion step S2, and a synthesis step S3.
[0044] In the pre-step S1, carbon dioxide in the environment
dissolves in water, and the two-phase coexistence aqueous solution
with carbon dioxide turns into a high temperature/high pressure
state. Specifically, the carbon dioxide can be an air pollutant
containing carbon in the environment. The gaseous carbon dioxide in
the air dissolves in liquid water to obtain the two-phase
coexistence aqueous solution with carbon dioxide (see chemical
equation 1 below).
CO.sub.2(g,T1)+H.sub.2O.sub.(.lamda.,T1).fwdarw.CO.sub.2(aq,T1)
(1)
[0045] wherein T1=298K, and P=1 atm.
[0046] Preferably, the two-phase coexistence aqueous solution is
pressurized at a normal temperature. The two-phase coexistence
aqueous solution turns into a high pressure state when its pressure
is above 1 atm. Then, the high pressure state two-phase coexistence
aqueous solution is heated to a high temperature, turning the
two-phase coexistence aqueous solution into a high temperature/high
pressure state (see chemical equation 2 below).
CO.sub.2(aq,T1,P1).fwdarw.CO.sub.2(aq,T2,P2) (2)
[0047] wherein T1=298K, P=1 atm, T2=400K, and P2=20 atm.
[0048] The term "normal temperature" referred to herein means 298K,
which can be appreciated by one skilled in the art. The term "high
temperature" referred to herein means a temperature higher than the
normal temperature. The term "normal pressure" referred to herein
means 1 atm, which can be appreciated by one skilled in the art.
The term "high pressure" referred to herein means a pressure higher
than the normal pressure.
[0049] As an example, in this embodiment, gaseous carbon dioxide at
1 atm and 298K dissolves in liquid water at 1 atm and 298K to
obtain two-phase coexistence aqueous solution at 1 atm and 298K.
The two-phase coexistence aqueous solution at 1 atm and 298K is
pressurized by a pump to 20 atm and 330K. The two-phase coexistence
aqueous solution is then gradually heated to 400K.
[0050] The conversion step S2 includes a separation step S21, a
reduction step S22, and an electrolysis step S23. Through the three
steps S1, S2, and S3, the two-phase coexistence aqueous solution is
heated and pressurized to the critical state, obtaining critical
state carbon monoxide and super critical state hydrogen.
[0051] Specifically, in the separation step S21, the two-phase
coexistence aqueous solution with carbon dioxide is heated to the
critical state where gas separates from liquid. Thus, gaseous
carbon dioxide and liquid water are separated from the two-phase
coexistence aqueous solution and are maintained in a high
temperature/high pressure state (see chemical equation 3
below).
CO.sub.2(aq,T2,P2).fwdarw.CO.sub.2(g,T2,P2)+H.sub.2O.sub.(.lamda.,T2,P2)
(3)
[0052] wherein T2=400K, and P2=20 atm.
[0053] After producing high temperature/high pressure gaseous
carbon dioxide in the separation step S21, the high
temperature/high pressure gaseous carbon dioxide is supplied with
electric current (preferably alternating current) and passes
through a heterophase catalyst (such as an oxide containing nickel,
ruthenium or titanium) in the reduction step S22. A reduction
reaction is, thus, undergone to obtain high temperature/high
pressure gaseous carbon monoxide. The high temperature/high
pressure gaseous carbon monoxide is then heated and pressurized to
produce critical state carbon monoxide (see chemical equations 4a
and 4b below).
2CO.sub.2(g,T2,P2).fwdarw.2CO.sub.(g,T2,P3)+O.sub.2(g,T2,P3)
(4a)
2CO.sub.(g,T2,P3).fwdarw.2CO.sub.(g,T3,P3) (4b)
[0054] wherein T2=400K, P3=30 atm, T3=672K, and P3=221 atm.
[0055] In the electrolysis step S23, the high temperature/high
pressure liquid water is firstly pressurized and then heated to
increase the pressure and temperature such that the high
temperature/high pressure liquid water immediately turns into
critical water after reaching the critical state. At this time, the
bond strength of the hydrogen bond of the critical water molecule
is significantly lower than that of the water molecule at normal
temperature/normal pressure. Thus, under low-current electrolysis,
the bond-dissociation energy of the critical water molecule can be
rapidly reached. As a result, the hydrogen molecules and oxygen
molecules in the critical water can easily be separated, producing
super critical state hydrogen and super critical state oxygen (see
chemical equations 5a and 5b below).
2H.sub.2O.sub.(.lamda.,T2,P2).fwdarw.2H.sub.2O.sub.(.lamda.,T3,P3)
(5a)
2H.sub.2O.sub.(.lamda.,T3,P3).fwdarw.2H.sub.2(g,T4,P4)+O.sub.2(g,T4,P4)
(5b)
[0056] wherein T3=672K, P3=221 atm, T4=700K, and P4=230 atm.
[0057] As an example, in this embodiment, the two-phase coexistence
aqueous solution at 20 atm and 400K is heated to 221 atm and 672K
such that super critical state carbon dioxide and water can be
produced from the two-phase coexistence aqueous solution. The
pressure and temperature of the gaseous carbon dioxide are 20 atm
and 400K, respectively. The pressure and temperature of the liquid
water are 20 atm and 400K, respectively. Next, alternating current
of 10-20 A is supplied to reduce the gaseous carbon dioxide at 20
atm and 400K to gaseous carbon monoxide at 30 atm and 400K. A pump
is used to heat and pressurize the gaseous carbon monoxide at 30
atm and 400K into critical state carbon monoxide (at 221 atm and
672K) that serves as one material for subsequent synthesis of
methanol.
[0058] On the other hand, a pump is used to compress liquid water
at 20 atm and 400K into liquid water at 221 atm. The liquid water
at 221 atm is gradually heated to 672K and turns into critical
water. Electric current is supplied to undergo electrolysis. After
reaching the bond-dissociation energy of the critical water, super
critical state hydrogen and super critical state oxygen can be
separated from the critical water. The hydrogen and oxygen are
maintained in the super critical state at 230 atm and 700K. The
super critical state hydrogen serves as another material for
subsequent synthesis of methanol. The super critical state oxygen
can be recovered and stored for use in other industrial
processes.
[0059] In the recovery step S3, the critical state carbon monoxide
and the super critical state hydrogen undergo a synthetic reaction
to produce gaseous methanol (see chemical equation 6 below).
Specifically, in this embodiment, the critical state carbon
monoxide at 221 atm and 672K reacts with the super critical state
gaseous hydrogen at 230 atm and 700K to produce gaseous methanol
after complete synthesis.
CO.sub.(g,T3,P3)+2H.sub.2(g,T4,P4).fwdarw.CH.sub.3OH.sub.(g,T5,P5)
(6)
[0060] wherein T5=730K, and P5=77 atm.
[0061] As mentioned above, in the method for producing methanol
according to the present invention, after dissolving gaseous carbon
dioxide in liquid water, the two-phase coexistence aqueous solution
can easily be pressurized and heated due to tighter molecular
alignment between liquid molecules than that between gaseous
molecules. Furthermore, after separation of gas from liquid, the
gaseous carbon dioxide can be reduced to gaseous carbon monoxide
under the action of alternating current, and the gaseous carbon
monoxide is heated and pressurized to turn into critical state
carbon monoxide. At the same time, the liquid water rapidly turns
into critical water under the second-time heating and
pressurization to reduce the bond strength between the hydrogen
atom and the oxygen atm. Thus, the bond-dissociation energy of
hydrogen molecules and oxygen molecules can easily be reached by
electrolysis, rapidly separating super critical state hydrogen and
super critical state oxygen from the critical water. Thus, the
production efficiency of super critical state hydrogen is
increased, and the critical state carbon monoxide reacts with the
super critical state hydrogen to produce methanol. As a result, the
method for producing methanol according to the present invention
increases the production efficiency of super critical state
hydrogen from electrolyzing water by using the critical state while
increasing the yield of super critical state hydrogen in a short
period of time. Through reaction of a large amount of super
critical state hydrogen and critical state carbon monoxide, the
production efficiency and yield of methanol can be increased.
[0062] FIG. 3 shows a device for producing methanol, which is a
preferred embodiment for producing methanol according to the
present invention for more particularly illustrating the method for
producing the methanol according to the present invention.
[0063] The device for producing methanol includes a mixing unit 1,
a conversion unit 2, and a synthesis unit 3. The units 1, 2, and 3
are connected by different pipes to form a continuous passage of
the device for producing methanol, which is described in detail as
follows.
[0064] The mixing unit 1 is used to mix the reactant materials to
assure that the reactant materials can flow into subsequent pipes
in a liquid state. In this embodiment, the mixing unit 1 is a
cooling/absorbing tower to assure that the carbon dioxide entering
the mixing unit 1 can completely dissolve in liquid water to save
the energy consumed in subsequent pressurization and heating.
[0065] The conversion unit 2 is connected by a pipe T1 to the
mixing unit 1. At least one pressurizing member P and at least one
heating member H are provided between the conversion unit 2 and the
mixing unit 1. The conversion unit 2 is used to output critical
gas. The pressurizing member P is used to compress the two-phase
coexistence aqueous solution flowing through the pipe T1. The
heating member H is connected to the pressurizing member P through
the pipe T1 to heat the two-phase coexistence aqueous solution
flowing from the mixing unit 1 through the pipe T1, turning the
two-phase coexistence aqueous solution into a high temperature/high
pressure state (even nearly the critical state) before entering the
conversion unit 2.
[0066] The conversion unit 2 includes a separator 21, a reducer 22,
and an electrolyser 23. The separator 21 is connected by the pipe
T1 to the mixing unit 1 to receive the two-phase coexistence
aqueous solution flowing through the pipe T1, separating and
outputting gaseous carbon dioxide and liquid water. The separator
21 is connected by a first branch pipe T21 to the reducer 22,
allowing flowing of the gaseous carbon dioxide from the separator
21. A second branch pipe T22 is connected between the electrolyser
23 and the separator 21 to introduce the liquid water flowing
through the second branch pipe T22 into the electrolyser 23. The
electrolyser 23 dissociates hydrogen and oxygen from the critical
water and separately outputs super critical state hydrogen and
super critical state oxygen. The two-phase coexistence aqueous
solution is obtained by dissolving carbon dioxide in water. The
pressurizing member P is preferably a pump.
[0067] The synthesis unit 3 is connected by another pipe to the
conversion unit 2, allowing a critical state gas to flow into the
synthesis unit 3. The synthesis unit 3 is connected to a gas outlet
pipe T30 for outputting a synthetic gas from the synthesis unit 3.
Specifically, the synthesis unit 3 is connected to the reducer 22
and the electrolyser 23 by two gas inlet pipes T31 and T32,
respectively. The gas inlet pipe T31 allows flow of gaseous carbon
monoxide from the reducer 22. The gas inlet pipe T32 allows flow of
super critical state hydrogen from the electrolyser 23. The two gas
inlet pipes T31 and T32 meet at the synthesis unit 3 to allow
synthesis of critical state carbon monoxide and super critical
state hydrogen to produce gaseous methanol that is outputted
through the gas outlet pipe T30.
[0068] FIG. 4 shows another embodiment of the present invention
using multiple-stage heating/pressurization. With reference to FIG.
4, another pressurizing member P1 and another heating member H1 are
provided on the second branch pipe T22. A further pressurizing
member P2 and a further heating member H2 are provided on the gas
inlet pipe T31.
[0069] By providing the pressurizing member P and the heating
member H on the pipe T1, the two-phase coexistence aqueous solution
flowing from the mixing unit 1 through the pipe T1 can be turned
into a high temperature/high pressure state so that the two-phase
coexistence aqueous solution can carry high heat energy into the
separator 21. At this time, the separator 21 receives the high
temperature/high pressure two-phase coexistence aqueous solution.
Furthermore, the separator 21 includes an auxiliary heating member
211 to provide the two-phase coexistence aqueous solution with more
heat energy to assure that the high temperature/high pressure
two-phase coexistence aqueous solution can reach the temperature
allowing separation of gas and liquid in the separator 21. Thus,
the separator 21 outputs gaseous carbon dioxide and liquid water.
The detailed structure and operational principle of separation of
gas and liquid of the separator 21 are known to one skilled in the
art and are, thus, not described in detail to avoid redundancy.
[0070] Furthermore, a gas collector (not shown) can be provided
above the separator 21 in this embodiment to absorb the gaseous
carbon dioxide. The gaseous carbon dioxide is guided by the first
branch pipe T21 into the reducer 22. The reducer 22 further
connects to a current supplier 221 that preferably supplies the
reducer 22 with sufficient alternating current to reduce the
gaseous carbon dioxide in the reducer 22 in gaseous carbon
monoxide.
[0071] Furthermore, the electrolyser 23 in this embodiment is
connected by the second branch pipe T22 to the separator 21, and
the pressurizing member P1 connected to the electrolyser 23
compresses the liquid water flowing from the separator 21 through
the second branch pipe T22 so that the liquid water can reach the
critical pressure value. The pressurizing member P1 is preferably a
pump merely for increasing the pressure of the liquid water while
maintaining the temperature of the liquid water. The heating member
H1 connected to the electrolyser 23 heats the liquid water to the
critical temperature value so that the liquid water turns into
critical water and flows into the electrolyser 23. At this time,
the electrolyser 23 is supplied with suitable current by another
current supplier 231 to reach the electrolysis energy level of the
critical water. By this arrangement, hydrogen molecules and oxygen
molecules are dissociated by the electrolyser 23 from the critical
water to respectively output super critical state hydrogen and
super critical state oxygen. The detailed structure and operational
principle of electrolysis of the electrolyser 23 are known to one
skilled in the art and are, thus, not described in detail to avoid
redundancy.
[0072] In this embodiment, by provision of the pressurizing member
P2 and the heating member H2 on the gas inlet pipe T31, the
synthesis unit 3 can turn the gaseous carbon monoxide flowing
through the gas inlet pipe T31 into critical state carbon monoxide.
Thus, the critical state carbon monoxide and the super critical
state hydrogen can react in the synthesis unit 3 to produce gaseous
methanol that is outputted via the gas outlet pipe T30 and that can
serve as fuel in industrial processes.
[0073] Furthermore, the electrolyser 23 can be connected by a gas
conveying pipe T23 to a storage tank 4 so that the super critical
state oxygen from the electrolyser 23 can be conveyed to and stored
in the storage tank 4 for other industrial processes. Further, a
plurality of heat dissipating members (not shown) can be mounted
between the electrolyser 23 and the storage tank 4 to achieve
energy saving effect.
[0074] The method for producing methanol according to the present
invention can be used on the device for producing methanol
according to the present invention with simple connection equipment
to increase the production efficiency of super critical state
hydrogen by electrolysis of liquid water. Furthermore, through
reaction of a large amount of super critical state hydrogen with
critical state carbon monoxide, the production efficiency and yield
of methanol can be increased. Further, the device for producing
methanol according to the present invention can reduce the energy
loss during the process. Further, the gaseous oxygen not used in
the reaction can be recovered and stored, further saving and
reusing energy.
[0075] In the method for producing methanol according to the
present invention, by using gaseous hydrogen obtained from
electrolyzing critical state liquid water that consumes less
energy, the electrolyzing efficiency of the liquid water can easily
be enhanced.
[0076] In the method for producing methanol according to the
present invention, the yield of gaseous hydrogen can be increased
to effectively increase the production efficiency of methanol.
[0077] In the device for producing methanol according to the
present invention, the energy consumed for producing the methanol
is reduced to effectively save energy.
[0078] In the device for producing methanol according to the
present invention, gaseous oxygen obtained from electrolyzing
critical state liquid water can be recovered and stored to reuse
energy.
[0079] Thus since the invention disclosed herein may be embodied in
other specific forms without departing from the spirit or general
characteristics thereof, some of which forms have been indicated,
the embodiments described herein are to be considered in all
respects illustrative and not restrictive. The scope of the
invention is to be indicated by the appended claims, rather than by
the foregoing description, and all changes which come within the
meaning and range of equivalency of the claims are intended to be
embraced therein.
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