CN209333721U - A kind of system of coal base combined production of methanol ethylene glycol - Google Patents
A kind of system of coal base combined production of methanol ethylene glycol Download PDFInfo
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- CN209333721U CN209333721U CN201821871744.0U CN201821871744U CN209333721U CN 209333721 U CN209333721 U CN 209333721U CN 201821871744 U CN201821871744 U CN 201821871744U CN 209333721 U CN209333721 U CN 209333721U
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Abstract
The utility model provides a kind of system of coal base combined production of methanol ethylene glycol, including coal gasification apparatus, gas purifying equipment, ethylene glycol synthesis device and methanol-fueled CLC equipment；Gas purifying equipment includes converting means, low temperature washing device for methanol and CO/H2Separator, converting means include heat recovery units and transformation and heat recovery units, and low temperature washing device for methanol includes non-transformed gas washing unit and conversion gas washing unit, CO/H2Separator includes CO cryogenic separation unit, pressure swing adsorption hydrogen production unit and resolution gas compression unit；Ethylene glycol synthesis device includes the dimethyl oxalate synthesizer and ethylene glycol synthesizer being sequentially communicated.Methanol-fueled CLC equipment includes the methanol synthesizer and methanol rectifying system being sequentially communicated.The utility model is that raw material carries out the coproduction of methanol ethylene glycol using coal, solves the problems such as device flexibility existing in the prior art is poor, economic benefit is lower effectively.
Description
Technical field
What it is the utility model relates to Chemical Engineering Technology and device field more particularly to a kind of coal base combined production of methanol ethylene glycol is
System.
Background technique
Ethylene glycol (EG) is most simple and most important aliphatic dihydroxy alcohol, and a kind of important Organic Chemicals.
Ethylene glycol is mainly for the production of polyethylene terephthalate (PET), antifreezing agent, unsaturated polyester resin (UPR) and lubrication
Agent, plasticizer, nonionic surfactant, explosive etc., purposes is very extensive.Ethylene glycol more than global half (China 90%)
Production of polyester all for China.With domestic polyester, the fast development in fiber product market, China has become world's ethylene glycol
Major producing country and maximum country of consumption, yield account for the 20% of world's total amount, consumption figure accounts for 50% or so of world's total amount.
Currently, industrially there are mainly two types of the ethylene glycol production technologies of realization business application: petroleum path and non-petroleum road
Line.So-called petroleum path, which refers to, obtains ethylene by PETROLEUM PROCESSING first, and ethylene produces ethylene oxide, finally by ethylene oxide
Hydration obtains the production technology of ethylene glycol.The economic benefit of this production technology is restricted by International Petroleum Price, is fluctuated larger.Institute
The Non oil-based route of meaning refers to that the route is for alleviating China's stone using one carbon atom compound as the process route of waste ethylene glycol
Oily disparities between supply and demand promote the development of steel, chemical industry, light industry and agricultural, it will play a significant role.
Methanol is important basic chemical industry raw material, and in chemical products, yield is only second to ethylene, propylene and benzene, occupies the
Four.It is other that methanol is widely used in organic intermediate, medicine, pesticide, dyestuff, coating, plastics, synthetic fibers, synthetic rubber etc.
In Chemical Manufacture, and it is used as solvent and industry and domestic fuel etc..By the downstream product of methanol production up to hundreds of, mainly spread out
Biology has: formaldehyde, methyl tertiary butyl ether(MTBE), acetic acid, methylamine, dimethyl ether, methyl formate, dimethyl suflfate, terephthalic acid (TPA) diformazan
Ester, methyl methacrylate, chloromethane alkanes, industry and domestic fuel etc..
The endowment of resources of " oil starvation, few gas, coal resources relative abundance " determines energy-consuming knot of the China based on coal
Structure, petroleum resources supportability are lower.Modern Coal-based Chemical industry can partially replace the consumption figure of China's oil and natural gas, promote
Into petrochemical industry raw material diversification, strategic support is provided for national energy security, provides emergency guarantee for Oil Safety.Coal chemical industry
The development of industry, to national energy consumption revolution strategy is implemented, protection environment has great importance.
Therefore, those skilled in the art is dedicated to the system for developing a kind of effective coal base combined production of methanol ethylene glycol.
Utility model content
The purpose of this utility model is to provide a kind of system of coal base combined production of methanol ethylene glycol, methanol and two kinds of ethylene glycol
The production of product carries out parallel, intercouples sufficiently energy-saving, not only improves effective gas component in abundant raw gas, also have
Conducive to the operational stability of the respective production technology of two kinds of finished products, methanol production enterprises numerous for China carry out product line expansions
It fills, positive directive significance is transformed, help enterprise to smoothly complete industry restructuring, better adapt to the needs in market.
In order to achieve the above objects and other related objects, what the utility model provided a kind of coal base combined production of methanol ethylene glycol is
System, including coal gasification apparatus, gas purifying equipment, ethylene glycol synthesis device and methanol-fueled CLC equipment；
The gas purifying equipment includes converting means, low temperature washing device for methanol and CO/H2Separator, the transformation dress
It sets including heat recovery units and transformation and heat recovery units, the low temperature washing device for methanol includes non-transformed gas washing unit and change
Ventilation washing unit, the CO/H2Separator includes CO cryogenic separation unit, pressure swing adsorption hydrogen production unit and resolution gas compression
Unit；The CO cryogenic separation unit is equipped with high-purity CO product gas outlet, flashed vapour outlet and hydrogen rich gas outlet；The transformation
Adsorption Hydrogen unit is equipped with high-purity H2Product gas outlet and analytical gas outlet；
The ethylene glycol synthesis device includes the dimethyl oxalate synthesizer and ethylene glycol synthesizer being sequentially communicated, institute
Stating dimethyl oxalate synthesizer includes the dimethyl oxalate synthesis unit and dimethyl oxalate rectification cell being sequentially communicated, described
Ethylene glycol synthesizer includes the ethylene glycol synthesis unit and ethylene glycol rectification cell being sequentially communicated；
Coal gasification apparatus outlet is divided into two accesses, an access successively with the heat recovery units, non-transformed gas washing
Unit, CO cryogenic separation unit, dimethyl oxalate synthesis unit, dimethyl oxalate rectification cell, ethylene glycol synthesis unit and second
Glycol rectification cell connection, another access successively with it is described transformation and heat recovery units, conversion gas washing unit, pressure-variable adsorption system
Hydrogen unit, ethylene glycol synthesis unit are connected to ethylene glycol rectification cell, wherein the high-purity CO product gas of CO cryogenic separation unit
Outlet is connected to the dimethyl oxalate synthesis unit, the high-purity H of pressure swing adsorption hydrogen production unit2Product gas outlet and the second
The flashed vapour outlet of the connection of glycol synthesis unit, CO cryogenic separation unit is connected to the conversion gas washing unit, CO deep cooling point
It exports from the hydrogen rich gas of unit and is connected to the pressure swing adsorption hydrogen production unit, the analytical gas outlet of pressure swing adsorption hydrogen production unit is successively
It is connected to the resolution gas compression unit and methanol-fueled CLC equipment；
The non-transformed gas washing unit is additionally provided with an access and is connected to the methanol-fueled CLC equipment, the transformation gas washing
Unit is additionally provided with an access and is connected to the methanol-fueled CLC equipment.
Preferably, the coal gasification apparatus includes the coal slurry preparation facilities and gasification installation being sequentially communicated, the gasification dress
It sets and two accesses is divided to be connected to respectively with heat recovery units and transformation and heat recovery units.
It is highly preferred that the coal gasification apparatus further includes pulp water processing unit, the gasification installation and pulp water processing unit
Connection, for handling the slag of gasification installation generation.
It is highly preferred that further including air separation plant, the air separation plant is closed with the gasification installation and dimethyl oxalate respectively
It is connected at unit.
Preferably, the gas purifying equipment further includes refrigerating plant, the refrigerating plant respectively with non-transformed gas washing
Unit is connected to conversion gas washing unit, provides cooling capacity to non-transformed gas washing unit and conversion gas washing unit.
Preferably, the gas purifying equipment further includes sulfur recovery facility, the sulfur recovery facility respectively with it is unchanged
Ventilation washing unit is connected to conversion gas washing unit, is produced for recycling non-transformed gas washing unit and conversion gas washing unit
Raw sulfur-rich tail gas.
Preferably, the low temperature washing device for methanol further includes Mathanol regenerating unit, the non-transformed gas washing unit and change
Ventilation washing unit is connected to Mathanol regenerating unit respectively, for Mathanol regenerating and is recycled.
Preferably, the methanol-fueled CLC equipment includes the methanol synthesizer and methanol rectifying system being sequentially communicated, described
It is logical that resolution gas compression unit, the non-transformed gas washing unit are additionally provided with an access, the conversion gas washing unit is additionally provided with one
Road is connected to the methanol synthesizer respectively.
Preferably, further include in following technical characteristic at least one of:
1) the methanol-fueled CLC equipment further includes hydrogen-carbon ratio detection device, and the hydrogen-carbon ratio detection device is set to methanol-fueled CLC
The entrance of device；
2) the methanol-fueled CLC equipment further includes fuel gas pipe network, and the fuel gas pipe network and methanol synthesizer connect
It is logical.
Preferably, further include in following technical characteristic at least one of:
1) CO/H2Separator further includes molecular sieve adsorber, and the molecular sieve is set to CO cryogenic separation unit and enters
Mouthful；
2) transformation and heat recovery units include the two-stage insulation change furnace being sequentially communicated；
3) the conversion gas washing unit further includes transformation flash gas compression component, and the transformation flash gas compression component is set
There are compression entrance and compression outlet, the flashed vapour outlet of CO cryogenic separation unit and the compression entrance of transformation flash gas compression component
The compression outlet of connection, transformation flash gas compression component is connected to pressure swing adsorption hydrogen production unit；
4) the ethylene glycol synthesis device further includes fuel gas pipe network, and the ethylene glycol synthesis unit and fuel gas pipe network connect
It is logical.
The utility model provides a kind of system of coal base combined production of methanol ethylene glycol, including coal gasification apparatus, gas purification are set
Standby, ethylene glycol synthesis device and methanol-fueled CLC equipment, not only system that is parallel but also intercoupling obtains two kinds of important chemical industry for use
Product methanol and ethylene glycol make full use of CO and H in raw gas2, traditional handicraft is compared, process is shortened, it is energy-saving, it starts
One new methanol ethylene glycol coproduction route.
Detailed description of the invention
Fig. 1 is shown as the system diagram of the coal base combined production of methanol ethylene glycol of the utility model.
Appended drawing reference:
A coal gasification apparatus
1 coal slurry preparation facilities
2 gasification installations
3 pulp water processing units
B gas purifying equipment
4 heat recovery units
5 transformation and heat recovery units
6 non-transformed gas washing units
7 conversion gas washing units
8 sulfur recovery facilities
9 CO cryogenic separation units
10 pressure swing adsorption hydrogen production units
16 resolution gas compression units
C ethylene glycol synthesis device
11 dimethyl oxalate synthesis units
13 dimethyl oxalate rectification cells
14 ethylene glycol synthesis units
15 ethylene glycol rectification cells
D methanol-fueled CLC equipment
17 methanol synthesizers
18 methanol rectifying systems
12 air separation plants
Specific embodiment
The embodiments of the present invention is illustrated by particular specific embodiment below, those skilled in the art can be by this
Content disclosed by specification understands other advantages and effect of the utility model easily.
Please refer to Fig. 1.It should be clear that this specification structure depicted in this specification institute accompanying drawings, ratio, size etc., only to cooperate
The revealed content of specification, so that those skilled in the art understands and reads, being not intended to limit the utility model can be real
The qualifications applied, therefore do not have technical essential meaning, the tune of the modification of any structure, the change of proportionate relationship or size
It is whole, in the case where not influencing the effect of the utility model can be generated and the purpose that can reach, it should all still fall in the utility model institute
The technology contents of announcement obtain in the range of capable of covering.Meanwhile in this specification it is cited as "upper", "lower", "left", "right",
The term of " centre " and " one " etc. is merely convenient to being illustrated for narration, rather than to limit the enforceable range of the utility model,
Its relativeness is altered or modified, under the content of no substantial changes in technology, when being also considered as the enforceable scope of the utility model.
As shown in Figure 1, a kind of system of coal base combined production of methanol ethylene glycol, including coal gasification apparatus A, gas purifying equipment B,
Ethylene glycol synthesis device C and methanol-fueled CLC equipment D；
The gas purifying equipment B includes converting means, low temperature washing device for methanol and CO/H2Separator, the transformation
Device includes heat recovery units 4 and transformation and heat recovery units 5, the low temperature washing device for methanol include non-transformed gas washing unit
6 and conversion gas washing unit 7, the CO/H2Separator includes CO cryogenic separation unit 9,10 and of pressure swing adsorption hydrogen production unit
Resolution gas compression unit 16；The CO cryogenic separation unit 9 is equipped with high-purity CO product gas outlet, flashed vapour outlet and hydrogen rich gas
Outlet；The pressure swing adsorption hydrogen production unit 10 is equipped with high-purity H2Product gas outlet and analytical gas outlet；
The ethylene glycol synthesis device C includes the dimethyl oxalate synthesizer and ethylene glycol synthesizer being sequentially communicated,
The dimethyl oxalate synthesizer includes the dimethyl oxalate synthesis unit 11 and dimethyl oxalate rectification cell being sequentially communicated
13, the ethylene glycol synthesizer includes the ethylene glycol synthesis unit 14 and ethylene glycol rectification cell 15 being sequentially communicated；
The outlet the coal gasification apparatus A is divided into two accesses, an access successively with the heat recovery units 4, non-transformed air purge
Wash unit 6, CO cryogenic separation unit 9, dimethyl oxalate synthesis unit 11, dimethyl oxalate rectification cell 13, ethylene glycol synthesis
Unit 14 is connected to ethylene glycol rectification cell 15, another access successively with it is described transformation and heat recovery units 5, transformation gas washing list
Member 7, pressure swing adsorption hydrogen production unit 10, ethylene glycol synthesis unit 14 are connected to ethylene glycol rectification cell 15, wherein CO cryogenic separation
The high-purity CO product gas outlet of unit 9 is connected to the dimethyl oxalate synthesis unit 11, pressure swing adsorption hydrogen production unit 10
High-purity H2Product gas outlet is connected to the ethylene glycol synthesis unit 14, the flashed vapour outlet of CO cryogenic separation unit 9 and institute
The connection of conversion gas washing unit 7 is stated, hydrogen rich gas outlet and the pressure swing adsorption hydrogen production unit 10 of CO cryogenic separation unit 9 connect
Logical, the analytical gas outlet of pressure swing adsorption hydrogen production unit 10 successively connects with the resolution gas compression unit 16 and methanol-fueled CLC equipment D
It is logical；
The non-transformed gas washing unit 6 is additionally provided with an access and is connected to the methanol-fueled CLC equipment D, the transformation air purge
It washs unit 7 and is additionally provided with an access and be connected to the methanol-fueled CLC equipment D.
The raw gas obtained through coal gasification apparatus A is divided into two-way when entering gas purifying equipment B, carries out depth change all the way
It changes and recuperation of heat, another way only carries out the recycling of heat；Gas washing is converted in the delivery outlet and low temperature washing device for methanol of conversion gas
7 input port of unit is connected, and unchanged ventilation delivery outlet is connected with 6 input port of gas washing unit non-transformed in low temperature washing device for methanol；
The non-transformed purified gas that non-transformed gas washing unit 6 exports is divided into two-way, isolates high-purity to CO cryogenic separation unit 9 all the way
CO gas, CO product gas outlet is connected with 11 input port of dimethyl oxalate synthesis unit, and another way is sent to methanol-fueled CLC equipment D
Entrance.The transformation purified gas that conversion gas washing unit 7 exports is again divided into two-way, produces height to pressure swing adsorption hydrogen production unit all the way
The H of purity2, H2Product gas outlet is connected with ethylene glycol synthesis unit input port, and another way is sent to methanol-fueled CLC equipment entrance.Become
Pressure Adsorption Hydrogen unit caused by resolution gas by resolution gas compression unit compression after send to methanol-fueled CLC equipment entrance, with
The non-transformed purified gas of non-transformed gas washing unit outlet and the transformation purified gas of conversion gas washing unit outlet are mixed into first
Alcohol synthesis device.
The gasification furnace with water-cooling wall and structure of boiler barrel, such as Jin Hualu can be used in the gasification furnace.
In a preferred embodiment, the coal gasification apparatus A includes the coal slurry preparation facilities 1 being sequentially communicated and gasification
Device 2, the gasification installation 2 are divided to two accesses to be connected to respectively with heat recovery units 4 and transformation and heat recovery units 5.
In a preferred embodiment, the coal gasification apparatus A further includes pulp water processing unit 3, the gasification installation 2
It is connected to pulp water processing unit 3, for handling the slag of gasification installation generation.
It in a preferred embodiment, further include air separation plant 12, the air separation plant 12 is filled with the gasification respectively
It sets 2 to be connected to dimethyl oxalate synthesis unit 11, provides required oxygen for gasification installation 2 and dimethyl oxalate synthesis unit 11
Gas.
In a preferred embodiment, the gas purifying equipment B further includes refrigerating plant, the refrigerating plant difference
It is connected to non-transformed gas washing unit 6 and conversion gas washing unit 7.The refrigerating plant is used for non-transformed gas washing unit 6
Cooling capacity, such as propylene refrigeration device are provided with conversion gas washing unit 7.
In a preferred embodiment, the gas purifying equipment B further includes sulfur recovery facility 8, and the sulphur returns
Receiving apparatus 8 is connected to non-transformed gas washing unit 6 and conversion gas washing unit 7 respectively, for recycling non-transformed gas washing unit 6
With sulfur-rich tail gas caused by conversion gas washing unit 7, sulphur is produced by sulfur recovery facility 8, is turned waste into wealth, ring is improved
Border.
In a preferred embodiment, the low temperature washing device for methanol further includes Mathanol regenerating unit, described non-transformed
Gas washing unit 6 and conversion gas washing unit 7 are connected to Mathanol regenerating unit respectively, for Mathanol regenerating and are recycled.
In a preferred embodiment, the methanol-fueled CLC equipment D includes 17 He of methanol synthesizer being sequentially communicated
Methanol rectifying system 18, the resolution gas compression unit 16, the non-transformed gas washing unit 6 are additionally provided with an access, the change
Ventilation washing unit 7 is additionally provided with an access and is connected to respectively with the methanol synthesizer 17.
Preferably, further include in following technical characteristic at least one of:
1) the methanol-fueled CLC equipment further includes hydrogen-carbon ratio detection device, and the hydrogen-carbon ratio detection device is set to methanol-fueled CLC
The entrance of device；
2) the methanol-fueled CLC equipment further includes fuel gas pipe network, and the fuel gas pipe network and methanol synthesizer connect
It is logical.
To control the concentration of impurity in methyl methanol syngas, while needing to convey a part of periodic off-gases into fuel gas pipe network,
To maintain the concentration of active principle in circulating air.
In a preferred embodiment, further include in following technical characteristic at least one of:
1) CO/H2Separator further includes molecular sieve adsorber, and the molecular sieve is set to CO cryogenic separation unit 9
Entrance, the molecular sieve adsorber can filter methanol and carbon dioxide in gas；
2) transformation and heat recovery units 5 include the two-stage insulation change furnace being sequentially communicated, and can complete CO transformation
While, it sufficiently recycles the different grades of steam of reaction heat by-product and is used for process units；
3) the conversion gas washing unit 7 further includes transformation flash gas compression component, the transformation flash gas compression component
Equipped with compression entrance and compression outlet, the flashed vapour outlet and the compression of transformation flash gas compression component of CO cryogenic separation unit 9
The compression outlet of entrance connection, transformation flash gas compression component is connected to pressure swing adsorption hydrogen production unit 10, the CO cryogenic separation
The flashed vapour that unit generates returns to the compression entrance of the transformation flash gas compression component of conversion gas washing unit, is sent after pressurization to change
Press Adsorption Hydrogen unit 10；
4) the ethylene glycol synthesis device C further includes fuel gas pipe network, the ethylene glycol synthesis unit 14 and fuel gas pipe
Net connection, in order to maintain synthesis system pressure, needs continuously to speed to put a part of gas to fuel gas pipe network.
Using the system of the utility model coal base combined production of methanol ethylene glycol, specifically comprise the following steps:
1) by raw material storing and transporting system Lai feed coal through scale feeder metering enter coal slurry preparation facilities 1 such as coal pulverizer
In, the coal slurry for wearing into certain particle size is mixed with a certain amount of water, concentration is about 60~61%.Water-coal-slurry is conveyed through high-pressure coal pulp pump
To such as gasification furnace process burner of gasification installation 2, the oxygen with air separation plant 12 is under conditions of about 6.7MPaG ,~1400 DEG C
Oxidation reaction occurs and generates raw gas.Raw gas after reaction successively passes through drum recycling heat, vaporization furnace bottom shock chamber swashs
It after cold, then send to gas purifying equipment B through dedusting, slag send to pulp water processing unit and is further processed；
2) about 242 DEG C, pressure about 6.5MPaG of the raw gas temperature from gasification unit are divided into before entering converting means
Two-way, entrance connects 4 progress raw gas heat recoveries of heat recovery units all the way, is in addition connected all the way with heat recovery units 5, into
Row depth conversion, converts H for CO as far as possible2, while recycling heat caused by conversion reaction；For respectively to conversion gas and not
Conversion gas carries out washing, purifying, and non-transformed gas washing unit 6 and conversion gas washing unit 7 is arranged in low temperature washing device for methanol, unchanged
Ventilation enters non-transformed gas washing unit 6, and conversion gas enters conversion gas washing unit 7, and crude synthesis gas enters washing for washing unit
After washing tower bottom, in Ta Nei and low-temp methanol (- 50 DEG C~-60 DEG C) counter current contacting, the H in gas is removed2S, COS and CO2, first
Alcohol enters system as absorbent in cold-zone, obtains recycling utilization in hot-zone, that is, Mathanol regenerating unit.Refrigerating plant such as third
Alkene refrigerating plant provides required cooling capacity for low temperature washing device for methanol；Low temperature washing device for methanol can generate H2S concentration about 30%
The acidity pneumatic transmission to sulfur recovery facility 8 is recycled the H in gas phase to avoid generation environment from polluting by sour gas2S produces molten sulfur
Or solid sulphur.
3) the non-transformed outlet of gas washing unit 6 is the highest purified gas of CO concentration in device, for abundant energy-saving, gas
Body a part is sent to methanol-fueled CLC equipment D entrance, and another part is sent to CO cryogenic separation unit 9, by CH in CO ice chest4、Ar
Equal impurity removal, the CO gas for obtaining deep purifying are used for dimethyl oxalate synthesis unit synthesizing dimethyl oxalate.CO deep cooling
The hydrogen rich gas that separative unit generates enters pressure swing adsorption hydrogen production unit recycling hydrogen, and flashed vapour then returns to low temperature washing device for methanol
The compression entrance for converting flash gas compression unit, send after pressurized to pressure swing adsorption hydrogen production unit 10.
4) outlet of conversion gas washing unit 7 is H in device2The highest purified gas of concentration, for abundant energy-saving, gas
A part is sent to methanol-fueled CLC equipment D entrance, remaining enters pressure swing adsorption hydrogen production unit purifying hydrogen of hydrogen.H2Preparation using become
Press absorbing process, unstripped gas of the hydrogen of obtained concentration >=99% as ethylene glycol synthetic reaction.Pressure swing adsorption hydrogen production unit
Resolution gas is sent after resolution gas compression unit is compressed to 5.5MPaG to methanol-fueled CLC equipment D, reaches the mesh for making full use of effective gas
's.
5) the CO gas of 9 exit concentration >=98.5% of CO cryogenic separation unit enters ethylene glycol synthesis device C mesoxalic acid two
The important process product methyl nitrite of another in methyl esters synthesis unit, with the unit is under the pressure of 0.4~0.5MPaG
Reaction generates thick dimethyl oxalate.To synthesize methyl nitrite, air separation plant 12 requires supplementation with fresh oxygen.Thick dimethyl oxalate
Dimethyl oxalate rectification cell 13 is subsequently entered to be purified.13 product essence dimethyl oxalate of oxalate rectification cell and transformation are inhaled
The H of attached Hydrogen Unit outlet2Thick ethylene glycol is generated in ethylene glycol synthesis unit 14, then in ethylene glycol rectification cell 15 most
The ethylene glycol product met the requirements eventually.In order to maintain synthesis system pressure, need continuously to speed to put a part of gas to fuel
Gas pipe network.
6) in low temperature washing device for methanol the non-transformed purified gas of non-transformed gas washing unit 6, from transformation gas washing
After the transformation purified gas of unit 7 mixes according to a certain percentage with the pressure-variable adsorption resolution gas from resolution gas compression unit 16,
Into methanol-fueled CLC equipment D.(H in gaseous mixture2-CO2)/(CO+CO2) maintain between 2.0~2.05, in methanol synthesizer
Methanol and other by-products are generated in methyl alcohol synthetic reactor in 17, crude carbinol, which subsequently enters methanol rectifying system 18, to carry out separation and mention
It is pure, obtain refined methanol.For the concentration of impurity in control methyl methanol syngas, needs continuously to convey a part into fuel gas pipe network and speed
It deflates, to maintain the concentration of active principle in circulating air.
The above embodiments are only illustrative of the principle and efficacy of the utility model, and not for limitation, this is practical new
Type.Any person skilled in the art can all carry out above-described embodiment under the spirit and scope without prejudice to the utility model
Modifications and changes.Therefore, such as those of ordinary skill in the art without departing from the revealed essence of the utility model
All equivalent modifications or change completed under mind and technical idea, should be covered by the claim of the utility model.
Claims (10)
1. a kind of system of coal base combined production of methanol ethylene glycol, which is characterized in that including coal gasification apparatus (A), gas purifying equipment
(B), ethylene glycol synthesis device (C) and methanol-fueled CLC equipment (D)；
The gas purifying equipment (B) includes converting means, low temperature washing device for methanol and CO/H2Separator, the converting means
It include non-transformed gas washing unit including heat recovery units (4) and transformation and heat recovery units (5), the low temperature washing device for methanol
(6) and conversion gas washing unit (7), the CO/H2Separator includes CO cryogenic separation unit (9), pressure swing adsorption hydrogen production list
First (10) and resolution gas compression unit (16)；The CO cryogenic separation unit (9) is equipped with high-purity CO product gas outlet, flashed vapour
Outlet and hydrogen rich gas outlet；The pressure swing adsorption hydrogen production unit (10) is equipped with high-purity H2Product gas outlet and analytical gas outlet；
The ethylene glycol synthesis device (C) includes the dimethyl oxalate synthesizer and ethylene glycol synthesizer being sequentially communicated, institute
Stating dimethyl oxalate synthesizer includes the dimethyl oxalate synthesis unit (11) and dimethyl oxalate rectification cell being sequentially communicated
(13), the ethylene glycol synthesizer includes the ethylene glycol synthesis unit (14) and ethylene glycol rectification cell (15) being sequentially communicated；
The coal gasification apparatus (A) outlet is divided into two accesses, an access successively with the heat recovery units (4), non-transformed air purge
Wash unit (6), CO cryogenic separation unit (9), dimethyl oxalate synthesis unit (11), dimethyl oxalate rectification cell (13), second
Glycol synthesis unit (14) is connected to ethylene glycol rectification cell (15), another access successively with the transformation and heat recovery units
(5), conversion gas washing unit (7), pressure swing adsorption hydrogen production unit (10), ethylene glycol synthesis unit (14) and ethylene glycol rectification cell
(15) it is connected to, wherein the high-purity CO product gas outlet of CO cryogenic separation unit (9) and the dimethyl oxalate synthesis unit
(11) it is connected to, the high-purity H of pressure swing adsorption hydrogen production unit (10)2Product gas outlet and the ethylene glycol synthesis unit (14) are even
Logical, the flashed vapour outlet of CO cryogenic separation unit (9) is connected to the conversion gas washing unit (7), CO cryogenic separation unit (9)
Hydrogen rich gas outlet be connected to the pressure swing adsorption hydrogen production unit (10), the analytical gas outlet of pressure swing adsorption hydrogen production unit (10) according to
It is secondary to be connected to the resolution gas compression unit (16) and methanol-fueled CLC equipment (D)；
The non-transformed gas washing unit (6) is additionally provided with an access and is connected to the methanol-fueled CLC equipment (D), the transformation air purge
It washs unit (7) and is additionally provided with an access and be connected to the methanol-fueled CLC equipment (D).
2. the system of coal base combined production of methanol ethylene glycol as described in claim 1, which is characterized in that the coal gasification apparatus (A)
Including the coal slurry preparation facilities (1) and gasification installation (2) being sequentially communicated, the gasification installation (2) is divided to two accesses to return respectively with heat
Unit (4) are received to be connected to transformation and heat recovery units (5).
3. the system of coal base combined production of methanol ethylene glycol as claimed in claim 2, which is characterized in that the coal gasification apparatus (A)
It further include pulp water processing unit (3), the gasification installation (2) is connected to pulp water processing unit (3), produces for handling gasification installation
Raw slag.
4. the system of coal base combined production of methanol ethylene glycol as claimed in claim 2, which is characterized in that further include air separation plant
(12), the air separation plant (12) is connected to the gasification installation (2) and dimethyl oxalate synthesis unit (11) respectively.
5. the system of coal base combined production of methanol ethylene glycol as described in claim 1, which is characterized in that the gas purifying equipment
It (B) further include refrigerating plant, the refrigerating plant connects with non-transformed gas washing unit (6) and conversion gas washing unit (7) respectively
It is logical, cooling capacity is provided to non-transformed gas washing unit (6) and conversion gas washing unit (7).
6. the system of coal base combined production of methanol ethylene glycol as described in claim 1, which is characterized in that the gas purifying equipment
(B) further include sulfur recovery facility (8), the sulfur recovery facility (8) respectively with non-transformed gas washing unit (6) and conversion gas
Washing unit (7) connection, for recycling sulfur-rich tail caused by non-transformed gas washing unit (6) and conversion gas washing unit (7)
Gas.
7. the system of coal base combined production of methanol ethylene glycol as described in claim 1, which is characterized in that the low temperature washing device for methanol
Further include Mathanol regenerating unit, the non-transformed gas washing unit (6) and conversion gas washing unit (7) respectively with Mathanol regenerating list
Member connection, for Mathanol regenerating and recycles.
8. the system of coal base combined production of methanol ethylene glycol as described in claim 1, which is characterized in that the methanol-fueled CLC equipment
It (D) include the methanol synthesizer (17) and methanol rectifying system (18) being sequentially communicated, the resolution gas compression unit (16), institute
State non-transformed gas washing unit (6) be additionally provided with an access, the conversion gas washing unit (7) be additionally provided with an access respectively with it is described
Methanol synthesizer (17) connection.
9. the system of coal base combined production of methanol ethylene glycol as claimed in claim 8, which is characterized in that further include following technical characteristic
At least one of in:
1) the methanol-fueled CLC equipment (D) further includes hydrogen-carbon ratio detection device, and the hydrogen-carbon ratio detection device is set to methanol-fueled CLC
The entrance of device (17)；
2) the methanol-fueled CLC equipment (D) further includes fuel gas pipe network, and the fuel gas pipe network and methanol synthesizer (17) are even
It is logical.
10. the system of coal base combined production of methanol ethylene glycol as described in claim 1, which is characterized in that further include that following technology is special
At least one of in sign:
1) CO/H2Separator further includes molecular sieve adsorber, and the molecular sieve is set to entering for CO cryogenic separation unit (9)
Mouthful；
2) transformation and heat recovery units (5) include the two-stage insulation change furnace being sequentially communicated；
3) the conversion gas washing unit (7) further includes transformation flash gas compression component, and the transformation flash gas compression component is set
There are compression entrance and compression outlet, the flashed vapour outlet and the compression of transformation flash gas compression component of CO cryogenic separation unit (9)
The compression outlet of entrance connection, transformation flash gas compression component is connected to pressure swing adsorption hydrogen production unit (10)；
4) the ethylene glycol synthesis device (C) further includes fuel gas pipe network, the ethylene glycol synthesis unit (14) and fuel gas pipe
Net connection.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113956131A (en) * | 2021-10-08 | 2022-01-21 | 华陆工程科技有限责任公司 | Method for realizing co-production of methanol/ethylene glycol through coupling of coal chemical industry and green hydrogen |
| CN114394883A (en) * | 2021-11-02 | 2022-04-26 | 华陆工程科技有限责任公司 | Method for preparing methanol by coupling gasification of pulverized coal waste boiler with green electricity and green hydrogen to achieve near-zero carbon emission |
-
2018
- 2018-11-13 CN CN201821871744.0U patent/CN209333721U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113956131A (en) * | 2021-10-08 | 2022-01-21 | 华陆工程科技有限责任公司 | Method for realizing co-production of methanol/ethylene glycol through coupling of coal chemical industry and green hydrogen |
| CN114394883A (en) * | 2021-11-02 | 2022-04-26 | 华陆工程科技有限责任公司 | Method for preparing methanol by coupling gasification of pulverized coal waste boiler with green electricity and green hydrogen to achieve near-zero carbon emission |
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