CN108101748A - Four tower triple effect methanol rectification energy-saving process methods and device - Google Patents
Four tower triple effect methanol rectification energy-saving process methods and device Download PDFInfo
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- CN108101748A CN108101748A CN201810101973.2A CN201810101973A CN108101748A CN 108101748 A CN108101748 A CN 108101748A CN 201810101973 A CN201810101973 A CN 201810101973A CN 108101748 A CN108101748 A CN 108101748A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 658
- 238000000034 method Methods 0.000 title claims abstract description 287
- 230000000694 effects Effects 0.000 title claims abstract description 106
- 230000008569 process Effects 0.000 title claims abstract description 85
- 238000004821 distillation Methods 0.000 claims abstract description 463
- 230000008901 benefit Effects 0.000 claims abstract description 50
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 126
- 239000007792 gaseous phase Substances 0.000 claims description 117
- 235000019441 ethanol Nutrition 0.000 claims description 69
- 239000000463 material Substances 0.000 claims description 68
- 239000007789 gas Substances 0.000 claims description 58
- 239000002351 wastewater Substances 0.000 claims description 57
- 238000007600 charging Methods 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 35
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 34
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 34
- 238000000605 extraction Methods 0.000 claims description 34
- 239000004571 lime Substances 0.000 claims description 34
- 239000002994 raw material Substances 0.000 claims description 29
- 239000001760 fusel oil Substances 0.000 claims description 28
- 239000012071 phase Substances 0.000 claims description 27
- 239000004291 sulphur dioxide Substances 0.000 claims description 24
- 238000009834 vaporization Methods 0.000 claims description 20
- 230000008016 vaporization Effects 0.000 claims description 20
- 238000010521 absorption reaction Methods 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 15
- 238000011084 recovery Methods 0.000 claims description 14
- 238000004064 recycling Methods 0.000 claims description 14
- 238000004519 manufacturing process Methods 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 7
- 239000003344 environmental pollutant Substances 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 7
- 231100000719 pollutant Toxicity 0.000 claims description 7
- 238000005192 partition Methods 0.000 claims description 6
- 239000004283 Sodium sorbate Substances 0.000 claims description 4
- 239000004301 calcium benzoate Substances 0.000 claims description 4
- 239000004303 calcium sorbate Substances 0.000 claims description 4
- 230000007812 deficiency Effects 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000004302 potassium sorbate Substances 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 3
- CUZMQPZYCDIHQL-VCTVXEGHSA-L calcium;(2s)-1-[(2s)-3-[(2r)-2-(cyclohexanecarbonylamino)propanoyl]sulfanyl-2-methylpropanoyl]pyrrolidine-2-carboxylate Chemical compound [Ca+2].N([C@H](C)C(=O)SC[C@@H](C)C(=O)N1[C@@H](CCC1)C([O-])=O)C(=O)C1CCCCC1.N([C@H](C)C(=O)SC[C@@H](C)C(=O)N1[C@@H](CCC1)C([O-])=O)C(=O)C1CCCCC1 CUZMQPZYCDIHQL-VCTVXEGHSA-L 0.000 claims 1
- 238000009833 condensation Methods 0.000 claims 1
- 230000005494 condensation Effects 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 13
- 230000007547 defect Effects 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 79
- 230000004069 differentiation Effects 0.000 description 51
- 230000010354 integration Effects 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- 239000004300 potassium benzoate Substances 0.000 description 4
- 239000004299 sodium benzoate Substances 0.000 description 4
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- 239000005711 Benzoic acid Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- 239000004284 Heptyl p-hydroxybenzoate Substances 0.000 description 2
- AMQJEAYHLZJPGS-UHFFFAOYSA-N N-Pentanol Chemical compound CCCCCO AMQJEAYHLZJPGS-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- PHTQWCKDNZKARW-UHFFFAOYSA-N isoamylol Chemical compound CC(C)CCO PHTQWCKDNZKARW-UHFFFAOYSA-N 0.000 description 2
- ZXEKIIBDNHEJCQ-UHFFFAOYSA-N isobutanol Chemical compound CC(C)CO ZXEKIIBDNHEJCQ-UHFFFAOYSA-N 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- TZIHFWKZFHZASV-UHFFFAOYSA-N methyl formate Chemical compound COC=O TZIHFWKZFHZASV-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- JYVLIDXNZAXMDK-UHFFFAOYSA-N pentan-2-ol Chemical compound CCCC(C)O JYVLIDXNZAXMDK-UHFFFAOYSA-N 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 241000403354 Microplus Species 0.000 description 1
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 1
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010960 commercial process Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- VLKZOEOYAKHREP-UHFFFAOYSA-N hexane Substances CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000004393 prognosis Methods 0.000 description 1
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to a kind of four tower triple effect methanol rectification energy-saving process methods and devices, it is the energy-saving process method and device for producing methanol by distillation process from crude carbinol.Whole device includes at least lightness-removing column（T201）, first rectifying column（T202）, Second distillation column（T203）, third distillation column（T204）Deng four towers and its corollary equipment.Present invention employs multitower multiple-effect the defects of being thermally integrated process, can overcoming the prior art, reduces operation energy consumption more than 30%, has significant practicability and economic benefit, has a extensive future.
Description
Technical field
The present invention relates to the energy-saving process methods and device of a kind of methanol rectification, it is that a kind of four tower triple effects of use are thermally integrated
Device produces the energy-saving process method and device of methanol from crude carbinol by distillation process.
Background technology
Methanol is a kind of important Organic Chemicals and novel energy fuel, in chemical industry, light industry and clean energy resource field
Tool has been widely used.In synthesizing methanol commercial process, the energy consumption of the subtractive process of crude carbinol is to influence methanol life
Produce one of key factor of cost.With the in short supply of the energy resources such as oil, coal, natural gas, environmental pollution and greenhouse effects
The problems such as getting worse, energy saving, the consumption reduction of the industries such as methanol become the key of Business survival and raising competitiveness, increasingly
Paid attention to be subject to each side.
Fig. 1 is a kind of four widely used at present towers（Three towers add a tower）Methanol rectification process, i.e., using pre-tower
Three towers such as T101, pressurizing tower T102, atmospheric tower T103 are further added by a recovery tower T104, produce national standard high-class product or American Standard AA
Grade methanol product.By pre-tower removed overhead light component, after 10 pressurized tower of prognosis crude carbinol and atmospheric tower rectifying, in pressurizing tower tower
Ejection material 24 and normal pressure column overhead discharging 14 obtain methanol product, atmospheric tower lateral line withdrawal function fusel 42 respectively.Pressurizing tower overhead materials
Expect that gas phase 21 is heated to atmospheric tower tower reactor.Rectifying column side line fusel 42 and normal pressure tower bottoms 15 are into recovery tower, by recycling column overhead
It is recycled methanol product 29, recovery tower lateral line withdrawal function fusel oil 30, recovery tower tower reactor waste discharge 33.Although this method skill
Art is ripe, but energy consumption is higher, and as unit scale increasingly increases, equipment scale seems more huge.To day
Construction, the economic stability operation of benefit enlargement methyl alcohol product installation are unfavorable.
The technique that Chinese patent CN 200610014321.2 discloses a kind of " rectification process of high purity methanol and preparation "
Method, CN 200610013269.9 are disclosed a kind of " double effect rectification for methanol energy-saving and water-saving system and technique ", in the core of the two
Hold all is on the basis of four tower rectifying process widely used at present, using in the lime set heat or system that heat steam
The heat exchange of portion's cold and hot liquids achievees the purpose that energy saving.Sensible heat transfer between obvious this material, for reducing entire rectifying system
The operation energy consumption of system, effect are very limited.
CN 200710067196.6 discloses " a kind of with the method for refining synthetic methanol being thermally integrated ", it is characterized in that
On the basis of four tower rectifying process widely used at present, pressurizing tower top gaseous phase is divided into two strands, respectively to pre-tower and first
Rectifying column provides heat.With respect to CN 200610014321.2 and CN 200610013269.9, this process has higher
Energy-saving effect.But since output methanol product, pressurizing tower do not belong to single-action to pre- column overhead for the energy that pre-tower provides in system
Methanol rectification process.Pressurizing tower, first rectifying column tower top all output methanol products, only pressurizing tower carry for first rectifying column in system
The energy of confession belongs to economic benefits and social benefits methanol rectification process, therefore, energy saving although this process is with certain improvement energy-saving effect
Effect is unsatisfactory.
CN 200710146369.3 discloses " pressure-reducing flow-reversing dual-purpose distillation method and equipment of a kind of refining crude methanol ",
It carries out the pressurizing tower during four tower rectifying widely used at present and the operating condition of first rectifying column and rectifying order
Optimization, the crude carbinol after pre-tower removes light component are introduced into vacuum rectification tower, rectification under vacuum tower bottoms enter back into it is micro- plus
Rectifying column is pressed, methanol product is obtained by the tower top of two towers.Micro- compression rectification column overhead gas phase gives vacuum rectification tower tower reactor reboiler
Heating.Although vacuum rectification tower is favourable compared with high methanol product purity for raising piece-rate system relative volatility, acquisition.But by
Relatively low in methanol boiling point, decompression operation can cause tower top temperature very low, and overhead condenser heat transfer temperature difference is substantially reduced, and is not only condensed
Device area is huge, simultaneously because vacuum system may cause the loss of methanol to increase.It is well known that this decompression operation process must
Significantly increasing for corresponding tower scale can so be caused.For the methanol device increasingly to maximize at present, this technique can cause tower
And heat transmission equipment scale is very huge.The essence of this technique still falls within the double-effect rectification process of traditional three-tower rectification, therefore not
Substantive breakthroughs can be obtained in terms of energy consumption is further reduced.Its operation energy consumption disregards pre-tower and recovery tower just has reached
0.916 ton of steam/ton methanol product, if being included in pre-tower and recovery tower energy consumption, operation energy consumption will be more than 1 ton of steam/ton first
Alcohol product.
The content of the invention
It is an object of the invention to provide a kind of four tower triple effect methanol rectification energy-saving process methods and devices, it is from thick first
The defects of producing the energy-saving process method of methanol in alcohol by distillation process, can overcoming the prior art, reduces operation energy consumption 30%
More than, there is significant practicability and economic benefit, have a extensive future.
The step of four towers triple effect methanol rectification energy-saving process method provided by the invention includes：
1）Including at least lightness-removing column T201, first rectifying column T202, Second distillation column T203, third distillation column T204 etc. four
Tower；
2）First rectifying column T202 side take-off gas phases enter lightness-removing column T201 tower reactors, and lightness-removing column T201 tower reactors are carried without reboiler
Heating load, lightness-removing column T201 tower reactor liquid phase materials enter first rectifying column T202.First rectifying column T202 side take-off gas phases
Position can be near the feed inlet or top of feed inlet or the lower section of feed inlet.
3）Third distillation column T204 lower parts use partition plate tower structure, and third distillation column T204 lower parts are divided by partition plate S204
Methanol stripping side L204 and ethyl alcohol rectifying side R204；
4）It is thermally integrated between first rectifying column T202, Second distillation column T203, tri- towers of third distillation column T204, Second distillation column
T203 top gaseous phases provide institute's calorific requirement as first rectifying column T202 tower reactor heat sources for first rectifying column T202；3rd
Rectifying column T204 top gaseous phases provide required heat as Second distillation column T203 tower reactor heat sources for Second distillation column T203
Amount；
5）Fixed gas 9 and light component 40 are discharged after the enrichment of lightness-removing column T201 tower tops；
6）From first rectifying column T202 tower tops or top side line, Second distillation column T203 tower tops or top side line, third distillation column
T204 tower tops or top side line produce refined methanol product respectively；
7）Waste water 32 is discharged from third distillation column T204 methanol strippings side L204 tower reactors；
8）From very low miscellaneous of side take-off methanol near the L204 feed inlets of third distillation column T204 methanol strippings side and ethanol content
Alcohol oil 28；
9）Recycling alcohol product 35 is produced from third distillation column T204 ethyl alcohol rectifying side R204 tower reactors.
By process provided by the invention, it is by following step：
Enter lightness-removing column T201 after crude carbinol raw material 1 is preheated.
Lightness-removing column T201 top gaseous phases 7 are directly returned through the condensed lime sets 8 of condenser of light component removal column E201 as phegma
To lightness-removing column T201 tower tops, fixed gas 9 discharges；First rectifying column T202 side take-offs gas phase 55 enters lightness-removing column T201 tower reactors,
Lightness-removing column T201 tower reactors provide heat without reboiler, and lightness-removing column T201 tower reactors liquid phase material 36 enters first rectifying column T202.
The position of first rectifying column T202 side take-off gas phases can be near feed inlet or the top of feed inlet, can also
It is the lower section of feed inlet.
First rectifying column T202 top gaseous phases 10 are divided to through the condensed lime sets 11 of first rectifying column condenser E202 for two strands,
One returns directly to first rectifying column T202 tower tops as phegma 12, and another burst of lime set 13 is as the extraction of refined methanol product；
First rectifying column T202 tops can also open up side take-off mouth and produce mouth as refined methanol product；First rectifying column T202 tower reactors
Material 14 enters Second distillation column T203.
The Second distillation column T203 and first rectifying column T202 is thermally integrated operation, Second distillation column T203 top gaseous phases 15
Into first rectifying column reboiler E203 shell sides, 15 condensed lime set 16 of top gaseous phase is divided to for two strands, one is as phegma
17 return directly to Second distillation column T203 tower tops, and another burst of lime set 18 is as the extraction of refined methanol product；Second distillation column T203
Top can also open up side take-off mouth and produce mouth as refined methanol product；Second distillation column T203 kettle materials 19 enter the 3rd
Rectifying column T204 methanol strippings side L204.
The third distillation column T204 and Second distillation column T203 is thermally integrated operation, third distillation column T204 top gaseous phases 20
Into Second distillation column reboiler E204 shell sides, 20 condensed lime set 21 of top gaseous phase is divided to for two strands, one is as phegma
22 return directly to third distillation column T204 tower tops, and another burst of lime set 23 is as the extraction of refined methanol product；Third distillation column T203
Top can also open up side take-off mouth and produce mouth as refined methanol product；Third distillation column T204 methanol strippings side L204 is fed
Mouthful nearby side take-off methanol and the very low fusel oil 27 of ethanol content；Third distillation column T204 methanol strippings side L204 tower reactor objects
Material 29 is produced as waste water, and third distillation column T204 ethyl alcohol rectifying side R204 kettle materials 34 are as recycling alcohol product extraction.
First rectifying column T202 overhead products 13 or tower top sideline product, Second distillation column T203 overhead products 18 or tower
Refined methanol product 24 after top sideline product, third distillation column T204 overhead products 23 or tower top side line product mix is through cold
But 26 carrying device of refined methanol product is obtained afterwards.
The waste water 31 that the waste water 29 produced from third distillation column T204 methanol strippings side L204 tower reactors obtains after cooling divides
For two strands, one is used as extraction water 33 to be back to lightness-removing column T201 tower tops as 32 carrying device of waste water, another strand.
The fusel oil 27 of third distillation column T204 methanol strippings side L204 side take-offs obtains fusel oil product after cooling
28 carrying devices.
The recycling ethyl alcohol 34 of third distillation column T204 ethyl alcohol rectifying side R204 tower reactors extraction is recycled ethyl alcohol after cooling
35 carrying device of product.
By process provided by the invention, in addition to production methanol is thermally integrated using above-mentioned four towers triple effect, can also deform
Flow, which is thermally integrated, for others produces methanol.
Deformation technique method one：In above-mentioned four tower, third distillation column T204 does not use diaphragm structure, and uses conventional knot
Structure, third distillation column T204 feed inlet more thans position, which produces, recycles ethyl alcohol 34, extraction fusel oil 27 in position below feed inlet, and the 3rd
Rectifying column T204 kettle materials 29 are produced as waste water.
Deformation technique method two：A stripper T206 is further added by above-mentioned four tower foundation, third distillation column T204 is not
Diaphragm structure is used, and using conventional structure.Five towers are thermally integrated using triple effect, and Second distillation column T203 top gaseous phases are as
One rectifying column T202 tower reactor heat sources, institute's calorific requirement is provided for first rectifying column T202；Third distillation column T204 top gaseous phases
As Second distillation column T203 tower reactor heat sources, institute's calorific requirement is provided for Second distillation column T203.
Deformation technique method three：In four towers and deformation technique method described in above-mentioned four tower and deformation technique method one
In five towers described in two, third distillation column T204 adds intermediate heater E220 near feed inlet, and form can be charging
Preheater or intermediate reboiler, heat source used can be that live steam, conduction oil or internal system generate
Material steam.
Deformation technique method four：The operating pressure of above-mentioned four tower is adjusted, is still thermally integrated operation for four tower triple effects.The
One rectifying column T202 operating pressures are constant, and Second distillation column T203 uses operation with high pressure, and third distillation column T204 is grasped using low pressure
Make.Third distillation column T204 top gaseous phases are provided as first rectifying column T202 tower reactor heat sources for first rectifying column T202
Institute's calorific requirement；Second distillation column T203 top gaseous phases are third distillation column as third distillation column T204 tower reactor heat sources
T204 provides institute's calorific requirement.
Deformation technique method five：The operating pressure of four towers described in deformation technique method one is adjusted, is still four towers
Triple effect is thermally integrated operation.First rectifying column T202 operating pressures are constant, and Second distillation column T203 uses operation with high pressure, the 3rd rectifying
Tower T204 is operated using low pressure.Third distillation column T204 top gaseous phases are as first rectifying column T202 tower reactor heat sources, for the
One rectifying column T202 provides institute's calorific requirement；Second distillation column T203 top gaseous phases heat heat as third distillation column T204 tower reactors
Source provides institute's calorific requirement for third distillation column T204.
Deformation technique method six：The operating pressure of five towers described in deformation technique method two is adjusted, is still five towers
Triple effect is thermally integrated operation.First rectifying column T202 operating pressures are constant, and Second distillation column T203 uses operation with high pressure, the 3rd rectifying
Tower T204 and stripper T206 is operated using low pressure.Third distillation column T204 top gaseous phases add as first rectifying column T202 tower reactors
Heat source provides institute's calorific requirement for first rectifying column T202；Second distillation column T203 top gaseous phases are as third distillation column T204
With stripper T206 tower reactor heat sources, institute's calorific requirement is provided for third distillation column T204 and stripper T206.
Deformation technique method seven：In four towers described in deformation technique method four and four towers described in deformation technique method five
And in five towers described in deformation technique method six, third distillation column T204 adds intermediate heater E220 near feed inlet,
Its form can be feed preheater or intermediate reboiler, and heat source used can be Second distillation column T203 tower overhead gases
The material steam that phase or live steam, conduction oil or internal system generate.
Deformation technique method eight：It reduces by a Second distillation column T203 on above-mentioned four tower foundation, becomes three tower economic benefits and social benefits heat
Integrated operation, third distillation column T204 top gaseous phases are first rectifying column as first rectifying column T202 tower reactor heat sources
T202 provides institute's calorific requirement.
Deformation technique method nine：Reduce by a Second distillation column on four tower foundations described in deformation technique method one
T203 becomes three tower economic benefits and social benefits and is thermally integrated operation, and third distillation column T204 top gaseous phases are heated as first rectifying column T202 tower reactors
Heat source provides institute's calorific requirement for first rectifying column T202.
Deformation technique method ten：Reduce by a Second distillation column on five tower foundations described in deformation technique method two
T203 becomes four tower economic benefits and social benefits and is thermally integrated operation, and third distillation column T204 top gaseous phases are heated as first rectifying column T202 tower reactors
Heat source provides institute's calorific requirement for first rectifying column T202.
Deformation technique method 11：In three towers described in deformation technique method eight and three described in deformation technique method nine
In four towers described in tower and deformation technique method ten, third distillation column T204 adds intermediate heater near feed inlet
E220, form can be feed preheater or intermediate reboiler, and heat source used can be live steam, conduction oil,
The material steam that either internal system generates.
Deformation technique method 12：In above-mentioned four tower, lightness-removing column T201 tower reactors add lightness-removing column reboiler E213, and first
Rectifying column T202 enters lightness-removing column T201 without side take-off gas phase.Four towers are thermally integrated using triple effect, Second distillation column T203
Top gaseous phase respectively as first rectifying column T202 tower reactors and lightness-removing column T201 tower reactor heat sources, be first rectifying column T202 and
Lightness-removing column T201 provides institute's calorific requirement respectively；Third distillation column T204 top gaseous phases heat heat as Second distillation column T203 tower reactors
Source provides institute's calorific requirement for Second distillation column T203.
Deformation technique method 13：A recovery tower T207, third distillation column T204 are further added by above-mentioned four tower foundation
Diaphragm structure is not used, and using conventional structure.First rectifying column T202, Second distillation column T203, third distillation column T204 tri-
It is thermally integrated between tower, Second distillation column T203 top gaseous phases are the first rectifying as first rectifying column T202 tower reactor heat sources
Tower T202 provides institute's calorific requirement；Third distillation column T204 top gaseous phases are as Second distillation column T203 tower reactor heat sources, for the
Two rectifying column T203 provide institute's calorific requirement；Second distillation column T203 or third distillation column T204 tower overhead gases can be used in recovery tower T207
Mutually as heat source either using other heat sources in system or using external heat source（Such as live steam）.
Deformation technique method 14：A water vaporization tower T208, third distillation column are further added by above-mentioned four tower foundation
T204 methanol strippings side L204 kettle materials enter at the top of water vaporization tower T208.When wastewater stripping tower reboiler heats vapour pressure
When power is enough, water vaporization tower T208 top gaseous phases 53 return to third distillation column T204 methanol strippings side L204 tower reactors；Work as waste water
During stripper reboiler heating steam pressure deficiency, water vaporization tower T208 top gaseous phases can return to Second distillation column T203 tower reactors
Or first rectifying column T202 tower reactors.Water vaporization tower T208 tower reactor extracted waste waters.Heat source used in wastewater stripping tower reboiler can be with
It is the material steam that live steam, conduction oil or internal system generate.
Deformation technique method 15：To the operating pressures of four towers described in deformation technique method 12 and be thermally integrated order into
Row adjustment, is still thermally integrated for four tower triple effects.First rectifying column T202 uses operation with high pressure, and Second distillation column T203 is grasped using low pressure
Make.First rectifying column T202 top gaseous phases are provided as Second distillation column T203 tower reactor heat sources for Second distillation column T203
Institute's calorific requirement；Second distillation column T203 top gaseous phases are as lightness-removing column T201 and third distillation column T204 tower reactor heat sources
Lightness-removing column T201 and third distillation column T204 provides institute's calorific requirement.
Deformation technique method 16：To the operating pressures of four towers described in deformation technique method 12 and be thermally integrated order into
Row adjustment, is still thermally integrated for four tower triple effects.First rectifying column T202 uses operation with high pressure, and third distillation column T204 is grasped using low pressure
Make.First rectifying column T202 top gaseous phases are provided as third distillation column T204 tower reactor heat sources for third distillation column T204
Institute's calorific requirement；Third distillation column T204 top gaseous phases are as lightness-removing column T201 and Second distillation column T203 tower reactor heat sources
Lightness-removing column T201 and Second distillation column T203 provides institute's calorific requirement.
By process provided by the invention, to reduce operation energy consumption, adoptable power-economizing method has：
1）Crude carbinol raw material can discharge wastewater heat exchange, crude carbinol raw material with third distillation column T204 methanol strippings side L204 tower reactors
It can also exchange heat with methanol product, crude carbinol raw material can also be changed with first rectifying column T202 or lightness-removing column T201 top gaseous phases
Heat；
2）The chargings of each tower such as first rectifying column T202, Second distillation column T203, third distillation column T204 or lightness-removing column T201 with
Heating vapour-condensing liquid exchanges heat.
The exemplary embodiment of heat exchange between this steam condensate and the charging of each tower has：
Steam condensate first exchanges heat with third distillation column T204 chargings, the T204 chargings of preheating third distillation column；
It feeds and exchanges heat with Second distillation column T203 again to the steam condensate after third distillation column T204 charging heat exchange, the second essence of preheating
Evaporate tower T203 chargings；
It feeds and exchanges heat with first rectifying column T202 again to the steam condensate after Second distillation column T203 charging heat exchange, the first essence of preheating
Evaporate tower T202 chargings；
It feeds and exchanges heat with lightness-removing column T201 again to the steam condensate after first rectifying column T202 charging heat exchange, preheating lightness-removing column T201
Charging.
Heat exchange mode between described steam condensate and the charging of each tower can be listed one kind in said combination,
Or the wherein combination of certain several heat exchange mode.Above-mentioned heat exchange mode is simply to four towers triple effect heat integration device provided by the invention
Carry out the supplement of the energy-saving process method of methanol rectification rather than the restriction to spirit of the present invention, those skilled in the relevant art
The permutation and combination of above-mentioned heat transfer process can be carried out according to common sense completely, the various differentiation technological processes being consequently formed all should
It is considered as in the spirit, scope and content of the present invention.
By process provided by the invention, may be selected to be thermally integrated in above-mentioned four towers triple effect（Or five tower triple effect be thermally integrated or
Three tower economic benefits and social benefits are thermally integrated）On the basis of be further added by an absorption tower T205, lightness-removing column T201 tail gas is washed in the T205 of absorption tower
Water goes out device again after absorbing, and to recycle methanol therein, improves methanol product yield, reduces pollutant in discharge fixed gas and contains
Amount.Increase absorption tower T205 is universal method, this general side can be used in either method provided by the invention or its deformation method
Method to improve methanol product yield, reduces pollutant load in discharge fixed gas.During using this universal method, extraction water can be with
A part 33 is into lightness-removing column T201 tower tops；Another part 37 is into absorption tower T205 tower tops；Extraction water can also be all into absorption tower
T205 tower tops.
By process provided by the invention, the first rectifying column T202 overhead products 13, Second distillation column T203
Overhead product 18, third distillation column T204 overhead products 23 can also be by each tower top side take-offs.
By process provided by the invention, heat source used in third distillation column the reboiler E205 and E206 can be
The material steam that live steam, conduction oil or internal system generate.
By process provided by the invention, lightness-removing column T201 tower reactors discharging can be introduced into first rectifying column T202 or
It is introduced into Second distillation column T203 or is introduced into third distillation column T204.
It is provided by the invention to be thermally integrated using four tower triple effects（Or five tower triple effect be thermally integrated or three tower economic benefits and social benefits are thermally integrated）Device
It carries out the process of methanol rectification and device can be used for AA grades of production national standard high-class product methanol, American Standard methanol products or other
The methanol product of specification.
By process provided by the invention, each tower typical operation conditions are：
Lightness-removing column T201 tower top operating pressures scope is 30~195kPa；
First rectifying column T202 tower top operating pressures scope is 30~195kPa；
Second distillation column T203 tower top operating pressures scope is 160~950kPa；
Third distillation column T204 tower top operating pressures scope is 310~1500kPa.
Unless otherwise specified, all pressure refer both to absolute pressure in the present invention.
By process provided by the invention, each tower preferred operations condition is：
Lightness-removing column T201 tower tops operating pressure is 80~150kpa, and tower top operation temperature is 50~85 DEG C, and tower reactor operation temperature is
55~90 DEG C；
First rectifying column T202 tower tops operating pressure is 80~180kpa, and tower top operation temperature is 50~90 DEG C, tower reactor operation temperature
It spends for 55~100 DEG C；
Second distillation column T203 tower tops operating pressure is 160~500kPa, and tower top operation temperature is 70~130 DEG C, tower reactor operation
Temperature is 75~140 DEG C.
Third distillation column T204 tower tops operating pressure is 400~900kPa, and tower top operation temperature is 90~150 DEG C, methanol
Stripping side L204 tower reactors operation temperature is 135~180 DEG C；Ethyl alcohol rectifying side R204 tower reactors operation temperature is 110~160 DEG C.
A kind of energy saver that methanol rectification is carried out using four tower triple effect heat integration devices provided by the invention is included：It is de- light
Four towers such as tower T201, first rectifying column T202, Second distillation column T203, third distillation column T204 and connecting pipeline.
The raw material crude carbinol feed line is respectively with feeding methanol preheater and charging waste water preheater cold side input port
It is connected.
Charging methanol preheater and charging waste water preheater cold side outlet port are connected in the middle part of lightness-removing column T201；Lightness-removing column T201
Tower top is connected with condenser of light component removal column, and condenser of light component removal column condensate outlet is connected with lightness-removing column T201 tower tops, condenser of light component removal column
Fixed gas outlet is connected with fixed gas discharge pipe line；Lightness-removing column T201 bottoms use a plurality of pipeline and first rectifying column T202 phases
Even.
First rectifying column T202 tower tops are connected with first rectifying column condenser, first rectifying column condenser condensate outlet difference
It is connected with first rectifying column T202 tower tops and charging methanol preheater hot side entrance；First rectifying column T202 side lines gas phase produces mouth
It is connected with lightness-removing column T201 tower reactors；First rectifying column T202 bottoms are smart with first rectifying column reboiler tube-side inlet and second respectively
It evaporates tower T203 to be connected, the outlet of first rectifying column reboiler tube side is connected to first rectifying column T202 tower reactors.
Second distillation column T203 tower tops are connected with first rectifying column reboiler shell side, first rectifying column reboiler shell side lime set
Outlet is connected respectively with Second distillation column T203 tower tops and charging methanol preheater hot side entrance；Second distillation column T203 bottoms point
It is not connected with Second distillation column reboiler tube-side inlet and third distillation column T204, Second distillation column reboiler tube side outlet connection
To Second distillation column T203 tower reactors.
Third distillation column T204 tower tops are connected with Second distillation column reboiler shell side, Second distillation column reboiler shell side lime set
Outlet is connected respectively with third distillation column T204 tower tops and charging methanol preheater hot side entrance；Third distillation column T204 methanol carries
Evaporate side L204 bottoms respectively with third distillation column methanol stripping side reboiler tube-side inlet and charging waste water preheater hot side entrance
It is connected, reboiler tube side outlet in third distillation column methanol stripping side is connected to third distillation column T204 methanol strippings side L204 towers
Kettle；Side take-off pipeline near third distillation column T204 methanol strippings side L204 chargings connects with fusel oil cooler hot side entrance
It connects；Third distillation column T204 ethyl alcohol rectifying side R204 bottoms respectively with third distillation column ethyl alcohol rectifying side reboiler tube-side inlet and
Ethyl alcohol cooler hot side entrance is connected, and reboiler tube side outlet in third distillation column ethyl alcohol rectifying side is connected to third distillation column T204
Ethyl alcohol rectifying side R204 tower reactors.
Charging methanol preheater hot side outlet is connected with methanol product cooler hot side entrance, methanol product cooler hot side
Outlet is connected with methanol product extraction pipeline.
Charging waste water preheater hot side outlet is connected with gaseous effluent cooler hot side entrance, gaseous effluent cooler hot side outlet difference
It is connected with lightness-removing column T201 tower tops and discharge of wastewater pipeline.
Fusel oil cooler hot side outlet is connected with fusel oil product extraction pipeline.
Ethyl alcohol cooler hot side outlet is connected with alcohol product extraction pipeline.
The present invention relates to the energy-saving process methods and device of a kind of methanol rectification, it is that a kind of four tower triple effects of use are thermally integrated
Device produces the energy-saving process method and device of methanol from crude carbinol by distillation process.Whole device includes at least lightness-removing column
Four towers such as T201, first rectifying column T202, Second distillation column T203, third distillation column T204 and its corollary equipment.The present invention
The defects of employing multitower and be thermally integrated process, can overcoming the prior art reduces operation energy consumption more than 30%, has notable
Practicability and economic benefit, have a extensive future.
Description of the drawings
Fig. 1 is four towers that prior art uses（Three towers add a tower）The flow chart of methanol rectification process.
Fig. 2 is the technological process that a kind of typical four towers triple effect heat integration device provided by the invention carries out methanol rectification
Figure.
Fig. 3 is a kind of differentiation process of Fig. 2, i.e. deformation technique method 1.During four towers triple effect shown in Fig. 2 is thermally integrated,
Third distillation column T204 does not use diaphragm structure, and using conventional structure, the extraction of third distillation column T204 feed inlet more thans position
Ethyl alcohol 34 is recycled, position produces fusel oil 27 below feed inlet, and third distillation column T204 kettle materials 29 are produced as waste water.
Fig. 4 is a kind of differentiation process of Fig. 2, i.e. deformation technique method two.Four towers triple effect shown in Fig. 2 is thermally integrated behaviour
It is changed to five tower triple effects and is thermally integrated production methanol.A stripper T206, third distillation column T204 are further added by four tower foundations
Diaphragm structure is not used, and using conventional structure.Five towers are thermally integrated using triple effect, Second distillation column T203 top gaseous phase conducts
First rectifying column T202 tower reactor heat sources provide institute's calorific requirement for first rectifying column T202；Third distillation column T204 tower overhead gases
Mutually as Second distillation column T203 tower reactor heat sources, institute's calorific requirement is provided for Second distillation column T203.
Fig. 5 is a kind of differentiation process of Fig. 2, i.e. deformation technique method three.Four towers triple effect shown in Fig. 2 is thermally integrated
In, third distillation column T204 adds intermediate heater E220 near feed inlet, and form can be feed preheater, can also
It is intermediate reboiler, heat source used can be the material steam that live steam, conduction oil or internal system generate.
Fig. 6 is a kind of differentiation process of Fig. 3, i.e. deformation technique method three.Four towers triple effect shown in Fig. 3 is thermally integrated
In, third distillation column T204 adds intermediate heater E220 near feed inlet, and form can be feed preheater, can also
It is intermediate reboiler, heat source used can be the material steam that live steam, conduction oil or internal system generate.
Fig. 7 is a kind of differentiation process of Fig. 4, i.e. deformation technique method three.Five towers triple effect shown in Fig. 4 is thermally integrated
In, third distillation column T204 adds intermediate heater E220 near feed inlet, and form can be feed preheater, can also
It is intermediate reboiler, heat source used can be the material steam that live steam, conduction oil or internal system generate.
Fig. 8 is a kind of differentiation process of Fig. 2, i.e. deformation technique method four.Four towers triple effect shown in Fig. 2 is thermally integrated
Operating pressure be adjusted, be still thermally integrated operation for four tower triple effects.First rectifying column T202 operating pressures are constant, the second rectifying
Tower T203 uses operation with high pressure, and third distillation column T204 is operated using low pressure.Third distillation column T204 top gaseous phases are as first
Rectifying column T202 tower reactor heat sources provide institute's calorific requirement for first rectifying column T202；Second distillation column T203 top gaseous phases are made
For third distillation column T204 tower reactor heat sources, institute's calorific requirement is provided for third distillation column T204.
Fig. 9 is a kind of differentiation process of Fig. 3, i.e. deformation technique method five.Four towers triple effect shown in Fig. 3 is thermally integrated
Operating pressure be adjusted, be still thermally integrated operation for four tower triple effects.First rectifying column T202 operating pressures are constant, the second rectifying
Tower T203 uses operation with high pressure, and third distillation column T204 is operated using low pressure.Third distillation column T204 top gaseous phases are as first
Rectifying column T202 tower reactor heat sources provide institute's calorific requirement for first rectifying column T202；Second distillation column T203 top gaseous phases are made
For third distillation column T204 tower reactor heat sources, institute's calorific requirement is provided for third distillation column T204.
Figure 10 is a kind of differentiation process of Fig. 4, i.e. deformation technique method six.Five towers triple effect shown in Fig. 4 heat is collected
Into operating pressure be adjusted, be still thermally integrated operation for five tower triple effects.First rectifying column T202 operating pressures are constant, the second essence
Tower T203 is evaporated to operate using low pressure using operation with high pressure, third distillation column T204 and stripper T206.Third distillation column T204 towers
As first rectifying column T202 tower reactor heat sources, institute's calorific requirement mutually is provided for first rectifying column T202 for top gas；Second distillation column
T203 top gaseous phases are third distillation column T204 and stripping as third distillation column T204 and stripper T206 tower reactor heat sources
Tower T206 provides institute's calorific requirement.
Figure 11 is a kind of differentiation process of Fig. 8, i.e. deformation technique method seven.Four towers triple effect shown in Fig. 8 is thermally integrated
In, third distillation column T204 adds intermediate heater E220 near feed inlet, and form can be feed preheater, can also
Intermediate reboiler, heat source used can be Second distillation column T203 top gaseous phases or live steam, conduction oil or
Person is the material steam that internal system generates.
Figure 12 is a kind of differentiation process of Fig. 9, i.e. deformation technique method seven.Four towers triple effect shown in Fig. 9 is thermally integrated
In, third distillation column T204 adds intermediate heater E220 near feed inlet, and form can be feed preheater, can also
Intermediate reboiler, heat source used can be Second distillation column T203 top gaseous phases or live steam, conduction oil or
Person is the material steam that internal system generates.
Figure 13 is a kind of differentiation process of Figure 10, i.e. deformation technique method seven.Five towers triple effect heat collection shown in Fig. 10
Cheng Zhong, third distillation column T204 add intermediate heater E220 near feed inlet, and form can be feed preheater, also may be used
To be intermediate reboiler, heat source used can be Second distillation column T203 top gaseous phases or live steam, conduction oil,
The material steam that either internal system generates.
Figure 14 is a kind of differentiation process of Fig. 2, i.e. deformation technique method eight.Collect in four towers triple effect shown in Fig. 2 heat
It reduces by a Second distillation column T203 on the basis of, becomes three tower economic benefits and social benefits and be thermally integrated operation, third distillation column T204 top gaseous phases
As first rectifying column T202 tower reactor heat sources, institute's calorific requirement is provided for first rectifying column T202.
Figure 15 is a kind of differentiation process of Fig. 3, i.e. deformation technique method nine.Collect in four towers triple effect shown in Fig. 3 heat
It reduces by a Second distillation column T203 on the basis of, becomes three tower economic benefits and social benefits and be thermally integrated operation, third distillation column T204 top gaseous phases
As first rectifying column T202 tower reactor heat sources, institute's calorific requirement is provided for first rectifying column T202.
Figure 16 is a kind of differentiation process of Fig. 4, i.e. deformation technique method ten.Five towers triple effect heat collection shown in Fig. 4
It reduces by a Second distillation column T203 on the basis of, becomes four tower economic benefits and social benefits and be thermally integrated operation, third distillation column T204 top gaseous phases
As first rectifying column T202 tower reactor heat sources, institute's calorific requirement is provided for first rectifying column T202.
Figure 17 is a kind of differentiation process of Figure 14, i.e. deformation technique method 11.Three tower economic benefits and social benefits heat shown in Figure 14
In integrated, third distillation column T204 adds intermediate heater E220 near feed inlet, and form can be feed preheater,
Can be intermediate reboiler, heat source used can be the material steam that live steam, conduction oil or internal system generate.
Figure 18 is a kind of differentiation process of Figure 15, i.e. deformation technique method 11.Three tower economic benefits and social benefits heat shown in Figure 15
In integrated, third distillation column T204 adds intermediate heater E220 near feed inlet, and form can be feed preheater,
Can be intermediate reboiler, heat source used can be the material steam that live steam, conduction oil or internal system generate.
Figure 19 is a kind of differentiation process of Figure 16, i.e. deformation technique method 11.Four tower economic benefits and social benefits heat shown in Figure 16
In integrated, third distillation column T204 adds intermediate heater E220 near feed inlet, and form can be feed preheater,
Can be intermediate reboiler, heat source used can be the material steam that live steam, conduction oil or internal system generate.
Figure 20 is a kind of differentiation process of Fig. 2, i.e. deformation technique method 12.Four towers triple effect heat collection shown in Fig. 2
Cheng Zhong, it is de- without the entrance of side take-off gas phase that lightness-removing column T201 tower reactors add lightness-removing column reboiler E213, first rectifying column T202
Light tower T201.Four towers are thermally integrated using triple effect, and Second distillation column T203 top gaseous phases are respectively as first rectifying column T202 towers
Kettle and lightness-removing column T201 tower reactor heat sources, institute's calorific requirement is provided for first rectifying column T202 and lightness-removing column T201 respectively；3rd
Rectifying column T204 top gaseous phases provide required heat as Second distillation column T203 tower reactor heat sources for Second distillation column T203
Amount.
Figure 21 is a kind of differentiation process of Fig. 2, i.e. deformation technique method 13.Four towers triple effect heat collection shown in Fig. 2
Production methanol is thermally integrated into five tower triple effects are changed to.A recovery tower T207, third distillation column T204 are further added by four tower foundations
Diaphragm structure is not used, and using conventional structure.First rectifying column T202, Second distillation column T203, third distillation column T204 tri-
It is thermally integrated between tower, Second distillation column T203 top gaseous phases are the first rectifying as first rectifying column T202 tower reactor heat sources
Tower T202 provides institute's calorific requirement；Third distillation column T204 top gaseous phases are as Second distillation column T203 tower reactor heat sources, for the
Two rectifying column T203 provide institute's calorific requirement；Second distillation column T203 or third distillation column T204 tower overhead gases can be used in recovery tower T207
Mutually as heat source either using other heat sources in system or using external heat source（Such as live steam）.
Figure 22 is a kind of differentiation process of Fig. 2, i.e. deformation technique method 14.Four towers triple effect heat collection shown in Fig. 2
Production methanol is thermally integrated into five tower triple effects are changed to.A water vaporization tower T208, third distillation column are further added by four tower foundations
T204 methanol strippings side L204 kettle materials enter at the top of water vaporization tower T208.When wastewater stripping tower reboiler heats vapour pressure
When power is enough, water vaporization tower T208 top gaseous phases 53 return to third distillation column T204 methanol strippings side L204 tower reactors；Work as waste water
During stripper reboiler heating steam pressure deficiency, water vaporization tower T208 top gaseous phases can return to Second distillation column T203 tower reactors
Or first rectifying column T202 tower reactors.Water vaporization tower T208 tower reactor extracted waste waters.Heat source used in wastewater stripping tower reboiler can be with
It is the material steam that live steam, conduction oil or internal system generate.
Figure 23 is a kind of differentiation process of Figure 20, i.e. deformation technique method 15.To four tower triple effects shown in Figure 20
The operating pressure being thermally integrated is adjusted with order is thermally integrated, and is still thermally integrated for four tower triple effects.First rectifying column T202 is using high
Press operation, Second distillation column T203 are operated using low pressure.First rectifying column T202 top gaseous phases are as Second distillation column T203 towers
Kettle heat source provides institute's calorific requirement for Second distillation column T203；Second distillation column T203 top gaseous phases are as lightness-removing column T201
With third distillation column T204 tower reactor heat sources, institute's calorific requirement is provided for lightness-removing column T201 and third distillation column T204.
Figure 24 is a kind of differentiation process of Figure 20, i.e. deformation technique method 16.To four tower triple effects shown in Figure 20
The operating pressure being thermally integrated is adjusted with order is thermally integrated, and is still thermally integrated for four tower triple effects.First rectifying column T202 is using high
Press operation, third distillation column T204 are operated using low pressure.First rectifying column T202 top gaseous phases are as third distillation column T204 towers
Kettle heat source provides institute's calorific requirement for third distillation column T204；Third distillation column T204 top gaseous phases are as lightness-removing column T201
With Second distillation column T203 tower reactor heat sources, institute's calorific requirement is provided for lightness-removing column T201 and Second distillation column T203.
Figure 25 is a kind of differentiation process of Fig. 2, is further added by the basis of four towers triple effect shown in Fig. 2 is thermally integrated operation
One absorption tower T205, lightness-removing column T201 tower tops tail gas is washed in the T205 of absorption tower after water absorbs goes out device again, with recycling
Methanol therein improves methanol product yield, reduces pollutant load in discharge fixed gas.
Figure 26 is a kind of differentiation process of Figure 20, is increased again on the basis of four tower triple effects shown in Figure 20 are thermally integrated operation
Add an absorption tower T205, lightness-removing column T201 tower tops tail gas is washed in the T205 of absorption tower after water absorbs goes out device again, to return
Methanol therein is received, improves methanol product yield, reduces pollutant load in discharge fixed gas.
Figure 27 is a kind of differentiation process of Figure 26, smart into first as the lightness-removing column T201 tower reactors discharging shown in Figure 26
Tower T202 is evaporated to be changed to be introduced into Second distillation column T203.
Specific embodiment
Specific embodiments of the present invention be explained in detail with reference to the accompanying drawings it is as follows, but for illustrative purposes only rather than limitation the present invention.
Unless otherwise specified, composition, the structure of the process equipments such as specifically used tower part, material are not specified in embodiment
（For connecting connecting pipeline between each tower part etc.）, reagent etc., be commercially available or the ordinary skill of this field
Personnel are obtained with well known method.Involved specific experiment method, operating condition, usually according to common process condition and hand
Volume described in condition or according to the condition proposed by manufacturer.
A kind of energy-saving process method that methanol rectification is carried out using four tower triple effect heat integration devices provided by the invention is included
Following steps：
1）Including at least lightness-removing column T201, first rectifying column T202, Second distillation column T203, third distillation column T204 etc. four
Tower；
2）First rectifying column T202 side take-off gas phases enter lightness-removing column T201 tower reactors, and lightness-removing column T201 tower reactors are carried without reboiler
Heating load, lightness-removing column T201 tower reactor liquid phase materials enter first rectifying column T202.First rectifying column T202 side take-off gas phases
Position can be near the feed inlet or top of feed inlet or the lower section of feed inlet.
3）Third distillation column T204 lower parts use partition plate tower structure, and third distillation column T204 lower parts are divided by partition plate S204
Methanol stripping side L204 and ethyl alcohol rectifying side R204；
4）It is thermally integrated between first rectifying column T202, Second distillation column T203, tri- towers of third distillation column T204, Second distillation column
T203 top gaseous phases provide institute's calorific requirement as first rectifying column T202 tower reactor heat sources for first rectifying column T202；3rd
Rectifying column T204 top gaseous phases provide required heat as Second distillation column T203 tower reactor heat sources for Second distillation column T203
Amount；
5）Fixed gas 9 and light component 40 are discharged after the enrichment of lightness-removing column T201 tower tops；
6）From first rectifying column T202 tower tops or top side line, Second distillation column T203 tower tops or top side line, third distillation column
T204 tower tops or top side line produce refined methanol product respectively；
7）Waste water 32 is discharged from third distillation column T204 methanol strippings side L204 tower reactors；
8）From very low miscellaneous of side take-off methanol near the L204 feed inlets of third distillation column T204 methanol strippings side and ethanol content
Alcohol oil 28；
9）Recycling alcohol product 35 is produced from third distillation column T204 ethyl alcohol rectifying side R204 tower reactors.
By process provided by the invention, comprise the concrete steps that：
Crude carbinol raw material 1 is divided to for two strand 2 and 3, and raw material 2 is raw material 4 after charging waste water preheater E208 preheatings, raw material 3 through into
It is raw material 5 after the E207 preheatings of material methanol preheater, enters lightness-removing column T201 after the mixing of raw material 4 and 5 after preheating for raw material 6.
Lightness-removing column T201 top gaseous phases 7 are directly returned through the condensed lime sets 8 of condenser of light component removal column E201 as phegma
To lightness-removing column T201 tower tops, fixed gas 9 discharges；First rectifying column T202 side take-offs gas phase 55 enters lightness-removing column T201 tower reactors,
Lightness-removing column T201 tower reactors provide heat without reboiler, and lightness-removing column T201 tower reactors liquid phase material 36 enters first rectifying column T202.
The position of first rectifying column T202 side take-off gas phases can be near feed inlet or the top of feed inlet, can also
It is the lower section of feed inlet.
First rectifying column T202 top gaseous phases 10 are divided to through the condensed lime sets 11 of first rectifying column condenser E202 for two strands,
One returns directly to first rectifying column T202 tower tops as phegma 12, another burst of lime set 13 as refined methanol product produce to
Feed methanol preheater E207；First rectifying column T202 kettle materials 14 enter Second distillation column T203.
The Second distillation column T203 and first rectifying column T202 is thermally integrated operation, Second distillation column T203 top gaseous phases 15
Into first rectifying column reboiler E203 shell sides, 15 condensed lime set 16 of top gaseous phase is divided to for two strands, one is as phegma
17 return directly to Second distillation column T203 tower tops, and another burst of lime set 18 is produced as refined methanol product to charging methanol preheater
E207；Second distillation column T203 kettle materials 19 enter third distillation column T204 methanol strippings side L204.
The third distillation column T204 and Second distillation column T203 is thermally integrated operation, third distillation column T204 top gaseous phases 20
Into Second distillation column reboiler E204 shell sides, 20 condensed lime set 21 of top gaseous phase is divided to for two strands, one is as phegma
22 return directly to third distillation column T204 tower tops, and another burst of lime set 23 is produced as refined methanol product to charging methanol preheater
E207；Third distillation column T204 methanol strippings side L204 feed inlets nearby side take-off methanol and the very low fusel oil of ethanol content
27 to fusel oil cooler E211；Third distillation column T204 methanol strippings side L204 kettle materials 29 are produced as waste water to charging
Waste water preheater E208, third distillation column T204 ethyl alcohol rectifying side R204 kettle materials 34 are produced as recycling alcohol product to second
Alcohol cooler E212.
First rectifying column T202 overhead products 13, Second distillation column T203 overhead products 18, third distillation column T204 tower tops
23 mixed refined methanol product 24 of product obtains refined methanol production after charging methanol preheater E207 exchanges heat with crude carbinol raw material 3
Product 25 obtain 26 carrying device of refined methanol product after being cooled down using methanol product cooler E209.
The waste water 29 of third distillation column T204 methanol strippings side L204 tower reactors extraction is through charging waste water preheater E208 and slightly
Methanol feedstock 2 obtains waste water 30 after exchanging heat, and the waste water 31 obtained after being cooled down using gaseous effluent cooler E210 is divided to for two strands, one
As 32 carrying device of waste water, another strand is used as extraction water 33 to be back to lightness-removing column T201 tower tops.
The fusel oil 27 of third distillation column T204 methanol strippings side L204 side take-offs is cooled down through fusel oil cooler E211
After obtain 28 carrying device of fusel oil product.
The recycling ethyl alcohol 34 of third distillation column T204 ethyl alcohol rectifying side R204 tower reactors extraction is cooled down through ethyl alcohol cooler E212
After be recycled 35 carrying device of alcohol product.
By process provided by the invention, typical crude carbinol raw material composition is：
Constituent mass percentage composition（%）
Carbon monoxide 0.07
Carbon dioxide 1.01
Methanol 96.04
Water 2.22
Ethyl alcohol 0.15
Dimethyl ether 0.10
Methyl formate 0.15
Acetone 0.01
Normal propyl alcohol 0.02
N-butanol 0.02
Isobutanol 0.03
N-amyl alcohol 0.01
Isoamyl alcohol 0.01
Sec-amyl alcohol 0.01
Pentane 0.03
N-hexane 0.08
Normal heptane 0.04
Total 100.00.
Above-mentioned raw materials compositing range does not form any limitation of the invention, and the present invention can be used for the crude carbinol of various compositions
The rectifying of raw material.
Application Example 1：
As shown in Fig. 2, crude carbinol raw material 1 is divided to for two strand 2 and 3, raw material 2 is raw material 4 after charging waste water preheater E208 preheatings,
Raw material 3 is raw material 5 after charging methanol preheater E207 is preheated, light into taking off for raw material 6 after the mixing of raw material 4 and 5 after preheating
Tower T201.
Lightness-removing column T201 top gaseous phases 7 are directly returned through the condensed lime sets 8 of condenser of light component removal column E201 as phegma
To lightness-removing column T201 tower tops, fixed gas 9 discharges；First rectifying column T202 side take-offs gas phase 55 enters lightness-removing column T201 tower reactors,
Lightness-removing column T201 tower reactors provide heat without reboiler, and lightness-removing column T201 tower reactors liquid phase material 36 enters first rectifying column T202.
The position of first rectifying column T202 side take-off gas phases can be near feed inlet or the top of feed inlet, can also
It is the lower section of feed inlet.
First rectifying column T202 top gaseous phases 10 are divided to through the condensed lime sets 11 of first rectifying column condenser E202 for two strands,
One returns directly to first rectifying column T202 tower tops as phegma 12, another burst of lime set 13 as refined methanol product produce to
Feed methanol preheater E207；First rectifying column T202 kettle materials 14 enter Second distillation column T203.
The Second distillation column T203 and first rectifying column T202 is thermally integrated operation, Second distillation column T203 top gaseous phases 15
Into first rectifying column reboiler E203 shell sides, 15 condensed lime set 16 of top gaseous phase is divided to for two strands, one is as phegma
17 return directly to Second distillation column T203 tower tops, and another burst of lime set 18 is produced as refined methanol product to charging methanol preheater
E207；Second distillation column T203 kettle materials 19 enter third distillation column T204 methanol strippings side L204.
The third distillation column T204 and Second distillation column T203 is thermally integrated operation, third distillation column T204 top gaseous phases 20
Into Second distillation column reboiler E204 shell sides, 20 condensed lime set 21 of top gaseous phase is divided to for two strands, one is as phegma
22 return directly to third distillation column T204 tower tops, and another burst of lime set 23 is produced as refined methanol product to charging methanol preheater
E207；Third distillation column T204 methanol strippings side L204 feed inlets nearby side take-off methanol and the very low fusel oil of ethanol content
27 to fusel oil cooler E211；Third distillation column T204 methanol strippings side L204 kettle materials 29 are produced as waste water to charging
Waste water preheater E208, third distillation column T204 ethyl alcohol rectifying side R204 kettle materials 34 are produced as recycling alcohol product to second
Alcohol cooler E212.
First rectifying column T202 overhead products 13, Second distillation column T203 overhead products 18, third distillation column T204 tower tops
23 mixed refined methanol product 24 of product obtains refined methanol production after charging methanol preheater E207 exchanges heat with crude carbinol raw material 3
Product 25 obtain 26 carrying device of refined methanol product after being cooled down using methanol product cooler E209.
The waste water 29 of third distillation column T204 methanol strippings side L204 tower reactors extraction is through charging waste water preheater E208 and slightly
Methanol feedstock 2 obtains waste water 30 after exchanging heat, and the waste water 31 obtained after being cooled down using gaseous effluent cooler E210 is divided to for two strands, one
As 32 carrying device of waste water, another strand is used as extraction water 33 to be back to lightness-removing column T201 tower tops.
The fusel oil 27 of third distillation column T204 methanol strippings side L204 side take-offs is cooled down through fusel oil cooler E211
After obtain 28 carrying device of fusel oil product.
The recycling ethyl alcohol 34 of third distillation column T204 ethyl alcohol rectifying side R204 tower reactors extraction is cooled down through ethyl alcohol cooler E212
After be recycled 35 carrying device of alcohol product.
It is hot used in third distillation column methanol stripping side reboiler E205 and third distillation column ethyl alcohol rectifying side reboiler E206
The material steam that source can be the conventional heat sources such as live steam, conduction oil or internal system generates.
The lime set for the live steam that system adds in can be respectively or successively each tower feeding preheating.
Preferred operations condition following present each tower in embodiment 1 is as follows：
Lightness-removing column T201 tower tops operating pressure is 80~150kpa, and tower top operation temperature is 50~85 DEG C, and tower reactor operation temperature is
55~90 DEG C；
First rectifying column T202 tower tops operating pressure is 80~180kpa, and tower top operation temperature is 50~90 DEG C, tower reactor operation temperature
It spends for 55~100 DEG C；
Second distillation column T203 tower tops operating pressure is 160~500kPa, and tower top operation temperature is 70~130 DEG C, tower reactor operation
Temperature is 75~140 DEG C.
Third distillation column T204 tower tops operating pressure is 400~900kPa, and tower top operation temperature is 90~150 DEG C, methanol
Stripping side L204 tower reactors operation temperature is 135~180 DEG C；Ethyl alcohol rectifying side R204 tower reactors operation temperature is 110~160 DEG C.
A kind of typical operation conditions and operation energy consumption following present each tower in embodiment 1 are as follows：
Lightness-removing column T201 tower tops operating pressure is 110kpa, and tower top operation temperature is 71 DEG C, and tower reactor operation temperature is 74 DEG C.
First rectifying column T202 tower tops operating pressure is 130kpa, and tower top operation temperature is 71 DEG C, and tower reactor operation temperature is
79℃；
Second distillation column T203 tower tops operating pressure is 320kPa, and tower top operation temperature is 97 DEG C, and tower reactor operation temperature is 109
℃。
Third distillation column T204 tower tops operating pressure is 750kPa, and tower top operation temperature is 126 DEG C, methanol stripping side L204
Tower reactor operation temperature is 169 DEG C；Ethyl alcohol rectifying side R204 tower reactors operation temperature is 139 DEG C.
Entire methanol rectifying system only third distillation column T204 tower bottom reboilers（E205、E206）Need external heating heat
Source, the equal utilisation system internal heat resource of heat source needed for remaining each reboiler and preheater etc. and steam condensate heating.
External heat source is considered that unit scale is by annual output AA grades of refined methanol products of 600,000 tons of American Standards by middle pressure steam（Behaviour
When making number by 7200 it is small when/year）, by four widely used at present tower methanol rectification techniques, the minimum steam consumption of methanol rectification process
It measures as 1 ton of steam/ton refined methanol product；The technique that methanol rectification is carried out using four towers triple effect heat integration device provided by the invention
Method, device steam consumption quantity are less than 58 ton hours, and steam mono-consumption is less than 0.7 ton of steam/ton refined methanol product.
Steam can be saved about every year：
（1-0.7）Ton/ton × 600,000 ton/year=180,000 ton/year.
By 150 yuan of calculating of steam per ton, steam expense can be saved every year：
180000 tons/year × 150 yuan/ton=27,000,000 yuan/year.
A kind of four towers triple effect heat integration device provided by the invention carries out the process and device of methanol rectification, has pole
Its significant economic benefit.
Application Example 2：
As shown in figure 3, it is a kind of differentiation process of Fig. 2, process difference relatively shown in Fig. 2 is：
During four towers triple effect shown in Fig. 2 is thermally integrated, third distillation column T204 does not use diaphragm structure, and uses conventional structure, the
Ethyl alcohol 34 is recycled in the extraction of three rectifying column T204 feed inlet more thans positions, and position produces fusel oil 27, the 3rd rectifying below feed inlet
Tower T204 kettle materials 29 are produced as waste water.
Application Example 3：
As shown in figure 4, it is a kind of differentiation process of Fig. 2, process difference relatively shown in Fig. 2 is：
Four towers triple effect shown in Fig. 2, which is thermally integrated operation and is changed to five tower triple effects, is thermally integrated production methanol.It is further added by four tower foundations
One stripper T206, third distillation column T204 do not use diaphragm structure, and using conventional structure.Five towers are using triple effect heat collection
Into Second distillation column T203 top gaseous phases are provided as first rectifying column T202 tower reactor heat sources for first rectifying column T202
Institute's calorific requirement；Third distillation column T204 top gaseous phases are Second distillation column as Second distillation column T203 tower reactor heat sources
T203 provides institute's calorific requirement.
Application Example 4：
As shown in figure 5, it is a kind of differentiation process of Fig. 2, process difference relatively shown in Fig. 2 is：
During four towers triple effect shown in Fig. 2 is thermally integrated, third distillation column T204 adds intermediate heater E220 near feed inlet,
Form can be feed preheater or intermediate reboiler, and heat source used can be live steam, conduction oil, either
The material steam that internal system generates.
Application Example 5：
As shown in fig. 6, it is a kind of differentiation process of Fig. 3, process difference relatively shown in Fig. 3 is：
During four towers triple effect shown in Fig. 3 is thermally integrated, third distillation column T204 adds intermediate heater E220 near feed inlet,
Form can be feed preheater or intermediate reboiler, and heat source used can be live steam, conduction oil, either
The material steam that internal system generates.
Application Example 6：
As shown in fig. 7, it is a kind of differentiation process of Fig. 4, process difference relatively shown in Fig. 4 is：
During five towers triple effect shown in Fig. 4 is thermally integrated, third distillation column T204 adds intermediate heater E220 near feed inlet,
Form can be feed preheater or intermediate reboiler, and heat source used can be live steam, conduction oil, either
The material steam that internal system generates.
Application Example 7：
As shown in figure 8, it is a kind of differentiation process of Fig. 2, process difference relatively shown in Fig. 2 is：
The operating pressure being thermally integrated to four towers triple effect shown in Fig. 2 is adjusted, and is still thermally integrated operation for four tower triple effects.First essence
It is constant to evaporate tower T202 operating pressures, Second distillation column T203 uses operation with high pressure, and third distillation column T204 is operated using low pressure.The
Three rectifying column T204 top gaseous phases provide required heat as first rectifying column T202 tower reactor heat sources for first rectifying column T202
Amount；Second distillation column T203 top gaseous phases are provided as third distillation column T204 tower reactor heat sources for third distillation column T204
Institute's calorific requirement.
Application Example 8：
As shown in figure 9, it is a kind of differentiation process of Fig. 3, process difference relatively shown in Fig. 3 is：
The operating pressure being thermally integrated to four towers triple effect shown in Fig. 3 is adjusted, and is still thermally integrated operation for four tower triple effects.First essence
It is constant to evaporate tower T202 operating pressures, Second distillation column T203 uses operation with high pressure, and third distillation column T204 is operated using low pressure.The
Three rectifying column T204 top gaseous phases provide required heat as first rectifying column T202 tower reactor heat sources for first rectifying column T202
Amount；Second distillation column T203 top gaseous phases are provided as third distillation column T204 tower reactor heat sources for third distillation column T204
Institute's calorific requirement.
Application Example 9：
As shown in Figure 10, it is a kind of differentiation process of Fig. 4, and process difference relatively shown in Fig. 4 is：
The operating pressure being thermally integrated to five towers triple effect shown in Fig. 4 is adjusted, and is still thermally integrated operation for five tower triple effects.First essence
It is constant to evaporate tower T202 operating pressures, Second distillation column T203 uses operation with high pressure, and third distillation column T204 and stripper T206 are adopted
It is operated with low pressure.Third distillation column T204 top gaseous phases are first rectifying column as first rectifying column T202 tower reactor heat sources
T202 provides institute's calorific requirement；Second distillation column T203 top gaseous phases are heated as third distillation column T204 and stripper T206 tower reactors
Heat source provides institute's calorific requirement for third distillation column T204 and stripper T206.
Application Example 10：
As shown in figure 11, it is a kind of differentiation process of Fig. 8, and process difference relatively shown in Fig. 8 is：
During four towers triple effect shown in Fig. 8 is thermally integrated, third distillation column T204 adds intermediate heater E220 near feed inlet,
Form can be feed preheater or intermediate reboiler, and heat source used can be Second distillation column T203 top gaseous phases,
It can also be the material steam that live steam, conduction oil or internal system generate.
Application Example 11：
As shown in figure 12, it is a kind of differentiation process of Fig. 9, and process difference relatively shown in Fig. 9 is：
During four towers triple effect shown in Fig. 9 is thermally integrated, third distillation column T204 adds intermediate heater E220 near feed inlet,
Form can be feed preheater or intermediate reboiler, and heat source used can be Second distillation column T203 top gaseous phases,
It can also be the material steam that live steam, conduction oil or internal system generate.
Application Example 12：
As shown in figure 13, it is a kind of differentiation process of Figure 10, and process difference relatively shown in Fig. 10 is：
During five towers triple effect shown in Fig. 10 is thermally integrated, third distillation column T204 adds intermediate heater E220 near feed inlet,
Its form can be feed preheater or intermediate reboiler, and heat source used can be Second distillation column T203 tower overhead gases
The material steam that phase or live steam, conduction oil or internal system generate.
Application Example 13：
As shown in figure 14, it is a kind of differentiation process of Fig. 2, and process difference relatively shown in Fig. 2 is：
It reduces by a Second distillation column T203 on the basis of four towers triple effect shown in Fig. 2 is thermally integrated, becomes three tower economic benefits and social benefits and be thermally integrated
Operation, third distillation column T204 top gaseous phases are carried as first rectifying column T202 tower reactor heat sources for first rectifying column T202
For institute's calorific requirement.
Application Example 14：
As shown in figure 15, it is a kind of differentiation process of Fig. 3, and process difference relatively shown in Fig. 3 is：
It reduces by a Second distillation column T203 on the basis of four towers triple effect shown in Fig. 3 is thermally integrated, becomes three tower economic benefits and social benefits and be thermally integrated
Operation, third distillation column T204 top gaseous phases are carried as first rectifying column T202 tower reactor heat sources for first rectifying column T202
For institute's calorific requirement.
Application Example 15：
As shown in figure 16, it is a kind of differentiation process of Fig. 4, and process difference relatively shown in Fig. 4 is：
Five towers triple effect shown in Fig. 4 reduces by a Second distillation column T203 on the basis of being thermally integrated, and becomes four tower economic benefits and social benefits and is thermally integrated
Operation, third distillation column T204 top gaseous phases are carried as first rectifying column T202 tower reactor heat sources for first rectifying column T202
For institute's calorific requirement.
Application Example 16：
As shown in figure 17, it is a kind of differentiation process of Figure 14, is with respect to the process difference shown in Figure 14：
During three tower economic benefits and social benefits shown in Figure 14 are thermally integrated, third distillation column T204 adds intermediate heater E220 near feed inlet,
Its form can be feed preheater or intermediate reboiler, heat source used can be live steam, conduction oil or
It is the material steam that internal system generates.
Application Example 17：
As shown in figure 18, it is a kind of differentiation process of Figure 15, is with respect to the process difference shown in Figure 15：
During three tower economic benefits and social benefits shown in Figure 15 are thermally integrated, third distillation column T204 adds intermediate heater E220 near feed inlet,
Its form can be feed preheater or intermediate reboiler, heat source used can be live steam, conduction oil or
It is the material steam that internal system generates.
Application Example 18：
As shown in figure 19, it is a kind of differentiation process of Figure 16, is with respect to the process difference shown in Figure 16：
During four tower economic benefits and social benefits shown in Figure 16 are thermally integrated, third distillation column T204 adds intermediate heater E220 near feed inlet,
Its form can be feed preheater or intermediate reboiler, heat source used can be live steam, conduction oil or
It is the material steam that internal system generates.
Application Example 19：
As shown in figure 20, it is a kind of differentiation process of Fig. 2, and process difference relatively shown in Fig. 2 is：
During four towers triple effect shown in Fig. 2 is thermally integrated, lightness-removing column T201 tower reactors add lightness-removing column reboiler E213, first rectifying column
T202 enters lightness-removing column T201 without side take-off gas phase.Four towers are thermally integrated using triple effect, Second distillation column T203 tower overhead gases
It is first rectifying column T202 and lightness-removing column mutually respectively as first rectifying column T202 tower reactors and lightness-removing column T201 tower reactor heat sources
T201 provides institute's calorific requirement respectively；Third distillation column T204 top gaseous phases are as Second distillation column T203 tower reactor heat sources
Second distillation column T203 provides institute's calorific requirement.
Application Example 20：
As shown in figure 21, it is a kind of differentiation process of Fig. 2, and process difference relatively shown in Fig. 2 is：
Four towers triple effect shown in Fig. 2, which is thermally integrated, to be changed to five tower triple effects and is thermally integrated production methanol.One is further added by four tower foundations
Recovery tower T207, third distillation column T204 do not use diaphragm structure, and using conventional structure.First rectifying column T202, the second essence
It evaporates and is thermally integrated between tower T203, tri- towers of third distillation column T204, Second distillation column T203 top gaseous phases are as first rectifying column
T202 tower reactor heat sources provide institute's calorific requirement for first rectifying column T202；Third distillation column T204 top gaseous phases are as second
Rectifying column T203 tower reactor heat sources provide institute's calorific requirement for Second distillation column T203；The second rectifying can be used in recovery tower T207
Tower T203 or third distillation column T204 top gaseous phases are warm either using other heat sources in system or using outside as heat source
Source（Such as live steam）.
Application Example 21：
As shown in figure 22, it is a kind of differentiation process of Fig. 2, and process difference relatively shown in Fig. 2 is：
Four towers triple effect shown in Fig. 2, which is thermally integrated, to be changed to five tower triple effects and is thermally integrated production methanol.One is further added by four tower foundations
Water vaporization tower T208, third distillation column T204 methanol strippings side L204 kettle materials enter at the top of water vaporization tower T208.When
When wastewater stripping tower reboiler heating steam pressure is enough, water vaporization tower T208 top gaseous phases 53 return to third distillation column T204
Methanol stripping side L204 tower reactors；When wastewater stripping tower reboiler heating steam pressure deficiency, water vaporization tower T208 tower overhead gases
It mutually can return to Second distillation column T203 tower reactors or first rectifying column T202 tower reactors.Water vaporization tower T208 tower reactor extracted waste waters.It is useless
Heat source used in water stripper reboiler can be the material steam that live steam, conduction oil or internal system generate.
Application Example 22：
As shown in figure 23, it is a kind of differentiation process of Figure 20, is with respect to the process difference shown in Figure 20：
The operating pressure that four tower triple effects shown in Figure 20 are thermally integrated with order is thermally integrated is adjusted, is still that four tower triple effects heat collects
Into.First rectifying column T202 uses operation with high pressure, and Second distillation column T203 is operated using low pressure.First rectifying column T202 tower overhead gases
Mutually as Second distillation column T203 tower reactor heat sources, institute's calorific requirement is provided for Second distillation column T203；Second distillation column T203
Top gaseous phase is lightness-removing column T201 and third distillation column as lightness-removing column T201 and third distillation column T204 tower reactor heat sources
T204 provides institute's calorific requirement.
Application Example 23：
As shown in figure 24, it is a kind of differentiation process of Figure 20, is with respect to the process difference shown in Figure 20：
The operating pressure that four tower triple effects shown in Figure 20 are thermally integrated with order is thermally integrated is adjusted, is still that four tower triple effects heat collects
Into.First rectifying column T202 uses operation with high pressure, and third distillation column T204 is operated using low pressure.First rectifying column T202 tower overhead gases
Mutually as third distillation column T204 tower reactor heat sources, institute's calorific requirement is provided for third distillation column T204；Third distillation column T204
Top gaseous phase is lightness-removing column T201 and Second distillation column as lightness-removing column T201 and Second distillation column T203 tower reactor heat sources
T203 provides institute's calorific requirement.
Application Example 24：
As shown in figure 25, it is a kind of differentiation process of Fig. 2, and process difference relatively shown in Fig. 2 is：
An absorption tower T205, lightness-removing column T201 tower top tails are further added by the basis of four towers triple effect shown in Fig. 2 is thermally integrated operation
Gas is washed in the T205 of absorption tower after water absorbs goes out device again, to recycle methanol therein, improves methanol product yield, reduces
Discharge pollutant load in fixed gas.
Application Example 25：
As shown in figure 26, it is a kind of differentiation process of Figure 20, is with respect to the process difference shown in Figure 20：
An absorption tower T205, lightness-removing column T201 tower top tails are further added by the basis of four tower triple effects shown in Figure 20 are thermally integrated operation
Gas is washed in the T205 of absorption tower after water absorbs goes out device again, to recycle methanol therein, improves methanol product yield, reduces
Discharge pollutant load in fixed gas.
Application Example 26：
As shown in figure 27, it is a kind of differentiation process of Figure 26, is with respect to the process difference shown in Figure 26：
It is discharged as the lightness-removing column T201 tower reactors shown in Figure 26 into first rectifying column T202 and is changed to be introduced into Second distillation column T203.
The present invention provides the energy-saving process methods and device of a kind of methanol rectification, it is a kind of using four tower triple effects heat collection
Produce the energy-saving process method and device of methanol by distillation process from crude carbinol into device.Whole device includes at least de- light
Four towers such as tower T201, first rectifying column T202, Second distillation column T203, third distillation column T204 and its corollary equipment.This hair
The defects of bright multitower that employs is thermally integrated process, can overcome the prior art reduces operation energy consumption more than 30%, has aobvious
The practicability and economic benefit of work.It is illustrated in conjunction with the embodiments, the personnel of association area completely can be according to the present invention
The method of offer suitably change or change with combining, to realize the technology.It should be strongly noted that all these pass through
Similar change or change are carried out to technological process provided by the invention with reconfiguring, is for a person skilled in the art
It will be apparent that it is considered as in the spirit, scope and content of the present invention.
Claims (10)
1. a kind of four tower triple effect methanol rectification energy-saving process methods, it is characterised in that including the step of：
1）Including at least lightness-removing column（T201）, first rectifying column（T202）, Second distillation column（T203）, third distillation column（T204）
Four towers；
2）First rectifying column（T202）Side take-off gas phase enters lightness-removing column（T201）Tower reactor, lightness-removing column（T201）Tower reactor is without again
It boils device and heat, lightness-removing column is provided（T201）Tower reactor liquid phase material enters first rectifying column（T202）；First rectifying column（T202）Side
The position of line extraction gas phase can be near feed inlet or the top of feed inlet or the lower section of feed inlet；
3）Third distillation column（T204）Lower part uses partition plate tower structure, partition plate（S204）By third distillation column（T204）Lower part every
For methanol stripping side（L204）With ethyl alcohol rectifying side（R204）；
4）First rectifying column（T202）, Second distillation column（T203）, third distillation column（T204）It is thermally integrated between three towers, the second essence
Evaporate tower（T203）Top gaseous phase is as first rectifying column（T202）Tower reactor heat source is first rectifying column（T202）Needed for offer
Heat；Third distillation column（T204）Top gaseous phase is as Second distillation column（T203）Tower reactor heat source is Second distillation column
（T203）Institute's calorific requirement is provided；
5）Through lightness-removing column（T201）Fixed gas is discharged after tower top enrichment（9）And light component（40）；
6）From first rectifying column（T202）Tower top or top side line, Second distillation column（T203）Tower top or top side line, the 3rd essence
Evaporate tower（T204）Tower top or top side line produce refined methanol product respectively；
7）From third distillation column（T204）Methanol stripping side（L204）Tower reactor discharges waste water（32）；
8）From third distillation column（T204）Methanol stripping side（L204）Nearby side take-off methanol and ethanol content are very low for feed inlet
Fusel oil（28）；
9）From third distillation column（T204）Ethyl alcohol rectifying side（R204）Tower reactor extraction recycling alcohol product（35）.
2. process described in accordance with the claim 1, it is characterised in that it is by following step：
Crude carbinol raw material（1）Enter lightness-removing column after preheated（T201）；
Lightness-removing column（T201）Top gaseous phase（7）Through condenser of light component removal column（E201）Condensed lime set（8）It is direct as phegma
It is back to lightness-removing column（T201）Tower top, fixed gas（9）Discharge；First rectifying column（T202）Side take-off gas phase（55）It is light into taking off
Tower（T201）Tower reactor, lightness-removing column（T201）Tower reactor provides heat, lightness-removing column without reboiler（T201）Tower reactor liquid phase material（36）
Into first rectifying column（T202）；First rectifying column（T202）Near the position of side take-off gas phase or feed inlet or into
The top of material mouth or the lower section of feed inlet；
First rectifying column（T202）Top gaseous phase（10）Through first rectifying column condenser（E202）Condensed lime set（11）It is divided into
Two strands, one is as phegma（12）Return directly to first rectifying column（T202）Tower top, another burst of lime set（13）As smart first
Alcohol product produces；First rectifying column（T202）Top opens up side take-off mouth as refined methanol product extraction mouth；First rectifying
Tower（T202）Kettle material（14）Into Second distillation column（T203）；
The Second distillation column（T203）With first rectifying column（T202）It is thermally integrated operation, Second distillation column（T203）Top gaseous phase
（15）Into first rectifying column reboiler（E203）Shell side, top gaseous phase（15）Condensed lime set（16）It is divided into two strands, one
As phegma（17）Return directly to Second distillation column（T203）Tower top, another burst of lime set（18）It is adopted as refined methanol product
Go out；Second distillation column（T203）Top opens up side take-off mouth as refined methanol product extraction mouth；Second distillation column（T203）
Kettle material（19）Into third distillation column（T204）Methanol stripping side（L204）；
The third distillation column（T204）With Second distillation column（T203）It is thermally integrated operation, third distillation column（T204）Top gaseous phase
（20）Into Second distillation column reboiler（E204）Shell side, top gaseous phase（20）Condensed lime set（21）It is divided into two strands, one
As phegma（22）Return directly to third distillation column（T204）Tower top, another burst of lime set（23）It is adopted as refined methanol product
Go out；Third distillation column（T203）Top opens up side take-off mouth as refined methanol product extraction mouth；Third distillation column（T204）
Methanol stripping side（L204）Feed inlet nearby side take-off methanol and the very low fusel oil of ethanol content（27）；Third distillation column
（T204）Methanol stripping side（L204）Kettle material（29）It is produced as waste water, third distillation column（T204）Ethyl alcohol rectifying side
（R204）Kettle material（34）As recycling alcohol product extraction；
First rectifying column（T202）Overhead product（13）Or tower top sideline product, Second distillation column（T203）Overhead product（18）
Or tower top sideline product, third distillation column（T204）Overhead product（23）Or the refined methanol production after the side line product mix of tower top
Product（24）Refined methanol product is obtained after cooling（26）Carrying device；
From third distillation column（T204）Methanol stripping side（L204）The waste water of tower reactor extraction（29）The waste water obtained after cooling
（31）It is divided into two strands, one is as waste water（32）Carrying device, another strand is used as extraction water（33）It is back to lightness-removing column（T201）
Tower top；
Third distillation column（T204）Methanol stripping side（L204）The fusel oil of side take-off（27）Fusel oil production is obtained after cooling
Product（28）Carrying device；
Third distillation column（T204）Ethyl alcohol rectifying side（R204）The recycling ethyl alcohol of tower reactor extraction（34）Second is recycled after cooling
Alcohol product（35）Carrying device.
3. process described in accordance with the claim 1, it is characterised in that：The process is removed using above-mentioned four towers triple effect heat collection
Flow production methanol is thermally integrated into producing outside methanol or being deformed into others：
Deformation technique method one：In four towers, third distillation column（T204）Diaphragm structure is not used, and uses conventional knot
Structure, third distillation column（T204）Feed inlet more than position extraction recycling ethyl alcohol（34）, the extraction of position below feed inlet fusel oil
（27）, third distillation column（T204）Kettle material（29）It is produced as waste water；
Deformation technique method two：A stripper is further added by four tower foundations（T206）, third distillation column（T204）
Diaphragm structure is not used, and using conventional structure；Five towers are thermally integrated using triple effect, Second distillation column（T203）Top gaseous phase is made
For first rectifying column（T202）Tower reactor heat source is first rectifying column（T202）Institute's calorific requirement is provided；Third distillation column
（T204）Top gaseous phase is as Second distillation column（T203）Tower reactor heat source is Second distillation column（T203）It is hot needed for offer
Amount；
Deformation technique method three：In four towers and deformation technique method 2 described in four towers and deformation technique method one
In five towers, third distillation column（T204）Intermediate heater is added near feed inlet（E220）, form can be into
Expect preheater or intermediate reboiler, heat source used can be that live steam, conduction oil or internal system generate
Material steam；
Deformation technique method four：The operating pressure of four towers is adjusted, is still thermally integrated operation for four tower triple effects；First
Rectifying column（T202）Operating pressure is constant, Second distillation column（T203）Using operation with high pressure, third distillation column（T204）Using low
Press operation, third distillation column（T204）Top gaseous phase is as first rectifying column（T202）Tower reactor heat source is first rectifying column
（T202）Institute's calorific requirement is provided；Second distillation column（T203）Top gaseous phase is as third distillation column（T204）Tower reactor heat source,
For third distillation column（T204）Institute's calorific requirement is provided；
Deformation technique method five：The operating pressure of four towers described in deformation technique method one is adjusted, is still four tower triple effects
It is thermally integrated operation, first rectifying column（T202）Operating pressure is constant, Second distillation column（T203）Using operation with high pressure, the 3rd rectifying
Tower（T204）It is operated using low pressure, third distillation column（T204）Top gaseous phase is as first rectifying column（T202）Tower reactor heating heat
Source is first rectifying column（T202）Institute's calorific requirement is provided；Second distillation column（T203）Top gaseous phase is as third distillation column
（T204）Tower reactor heat source is third distillation column（T204）Institute's calorific requirement is provided；
Deformation technique method six：The operating pressure of five towers described in deformation technique method two is adjusted, is still five tower triple effects
It is thermally integrated operation, first rectifying column（T202）Operating pressure is constant, Second distillation column（T203）Using operation with high pressure, the 3rd rectifying
Tower（T204）And stripper（T206）It is operated using low pressure, third distillation column（T204）Top gaseous phase is as first rectifying column
（T202）Tower reactor heat source is first rectifying column（T202）Institute's calorific requirement is provided；Second distillation column（T203）Top gaseous phase is made
For third distillation column（T204）And stripper（T206）Tower reactor heat source is third distillation column（T204）And stripper（T206）
Institute's calorific requirement is provided；
Deformation technique method seven：In four towers described in deformation technique method four and four towers described in deformation technique method five and
In five towers described in deformation technique method six, third distillation column（T204）Intermediate heater is added near feed inlet（E220）,
Its form can be feed preheater or intermediate reboiler, and heat source used can be Second distillation column（T203）Tower top
The material steam that gas phase or live steam, conduction oil or internal system generate；
Deformation technique method eight：Reduce by a Second distillation column on four tower foundations（T203）, become three tower economic benefits and social benefits heat
Integrated operation, third distillation column（T204）Top gaseous phase is as first rectifying column（T202）Tower reactor heat source is the first rectifying
Tower（T202）Institute's calorific requirement is provided；
Deformation technique method nine：Reduce by a Second distillation column on four tower foundations described in deformation technique method one（T203）,
Become three tower economic benefits and social benefits and be thermally integrated operation, third distillation column（T204）Top gaseous phase is as first rectifying column（T202）Tower reactor heating heat
Source is first rectifying column（T202）Institute's calorific requirement is provided；
Deformation technique method ten：Reduce by a Second distillation column on five tower foundations described in deformation technique method two（T203）,
Become four tower economic benefits and social benefits and be thermally integrated operation, third distillation column（T204）Top gaseous phase is as first rectifying column（T202）Tower reactor heating heat
Source is first rectifying column（T202）Institute's calorific requirement is provided；
Deformation technique method 11：Three towers described in deformation technique method eight and three towers described in deformation technique method nine with
And in four towers described in deformation technique method ten, third distillation column（T204）Intermediate heater is added near feed inlet
（E220）, form or feed preheater or intermediate reboiler, heat source used can be live steam, conduction oil or
It is the material steam that internal system generates；
Deformation technique method 12：In four towers, lightness-removing column（T201）Tower reactor adds lightness-removing column reboiler（E213）, the
One rectifying column（T202）Enter lightness-removing column without side take-off gas phase（T201）, four towers are thermally integrated using triple effect, the second rectifying
Tower（T203）Top gaseous phase is respectively as first rectifying column（T202）Tower reactor and lightness-removing column（T201）Tower reactor heat source is first
Rectifying column（T202）And lightness-removing column（T201）Institute's calorific requirement is provided respectively；Third distillation column（T204）Top gaseous phase is as the second essence
Evaporate tower（T203）Tower reactor heat source is Second distillation column（T203）Institute's calorific requirement is provided；
Deformation technique method 13：A recovery tower is further added by four tower foundations（T207）, third distillation column
（T204）Diaphragm structure is not used, and using conventional structure, first rectifying column（T202）, Second distillation column（T203）, the 3rd essence
Evaporate tower（T204）It is thermally integrated between three towers, Second distillation column（T203）Top gaseous phase is as first rectifying column（T202）Tower reactor heats
Heat source is first rectifying column（T202）Institute's calorific requirement is provided；Third distillation column（T204）Top gaseous phase is as Second distillation column
（T203）Tower reactor heat source is Second distillation column（T203）Institute's calorific requirement is provided；Recovery tower（T207）The second rectifying can be used
Tower（T203）Or third distillation column（T204）Top gaseous phase is as heat source either using other heat sources in system or using outer
Portion's heat source；
Deformation technique method 14：A water vaporization tower is further added by four tower foundations（T208）, third distillation column
（T204）Methanol stripping side（L204）Kettle material enters water vaporization tower（T208）Top, when wastewater stripping tower reboiler heats
When steam pressure is enough, water vaporization tower（T208）Top gaseous phase（53）Return to third distillation column（T204）Methanol stripping side
（L204）Tower reactor；When wastewater stripping tower reboiler heating steam pressure deficiency, water vaporization tower（T208）Top gaseous phase can return
Return Second distillation column（T203）Tower reactor or first rectifying column（T202）Tower reactor, water vaporization tower（T208）Tower reactor extracted waste water；It is useless
Heat source used in water stripper reboiler can be the material steam that live steam, conduction oil or internal system generate；
Deformation technique method 15：The operating pressure of four towers described in deformation technique method 12 is adjusted with order is thermally integrated
It is whole, still it is thermally integrated for four tower triple effects；First rectifying column（T202）Using operation with high pressure, Second distillation column（T203）It is grasped using low pressure
Make, first rectifying column（T202）Top gaseous phase is as Second distillation column（T203）Tower reactor heat source is Second distillation column
（T203）Institute's calorific requirement is provided；Second distillation column（T203）Top gaseous phase is as lightness-removing column（T201）And third distillation column（T204）
Tower reactor heat source is lightness-removing column（T201）And third distillation column（T204）Institute's calorific requirement is provided；
Deformation technique method 16：The operating pressure of four towers described in deformation technique method 12 is adjusted with order is thermally integrated
It is whole, it is still thermally integrated for four tower triple effects, first rectifying column（T202）Using operation with high pressure, third distillation column（T204）It is grasped using low pressure
Make, first rectifying column（T202）Top gaseous phase is as third distillation column（T204）Tower reactor heat source is third distillation column
（T204）Institute's calorific requirement is provided；Third distillation column（T204）Top gaseous phase is as lightness-removing column（T201）And Second distillation column（T203）
Tower reactor heat source is lightness-removing column（T201）And Second distillation column（T203）Institute's calorific requirement is provided.
4. according to any processes of claim 1-3, it is characterised in that the power-economizing method selection of use：
1）Crude carbinol raw material can be with third distillation column（T204）Methanol stripping side（L204）Tower reactor discharges wastewater heat exchange, crude carbinol
Raw material can also exchange heat with methanol product, and crude carbinol raw material can also be with first rectifying column（T202）Or lightness-removing column（T201）Tower top
Gas phase exchanges heat；
2）First rectifying column（T202）, Second distillation column（T203）, third distillation column（T204）Or lightness-removing column（T201）Etc. each tower
Charging and heating vapour-condensing liquid exchange heat.
5. according to any processes of claim 1-3, it is characterised in that：It is thermally integrated or five in the four towers triple effect
Tower triple effect is thermally integrated or three tower economic benefits and social benefits be thermally integrated on the basis of be further added by an absorption tower（T205）, lightness-removing column（T201）Tail gas exists
Absorption tower（T205）Interior washed water goes out device again after absorbing, and to recycle methanol therein, improves methanol product yield, reduces row
Put pollutant load in fixed gas.
6. according to any processes of claim 1-3, it is characterised in that：Third distillation column reboiler（E205、
E206）Heat source used can be the material steam that live steam, conduction oil or internal system generate.
7. process described in accordance with the claim 3, it is characterised in that：Lightness-removing column（T201）Tower reactor discharging is introduced into the first essence
Evaporate tower（T202）Or it is introduced into Second distillation column（T203）Or it is introduced into third distillation column（T204）.
8. according to the process described in claim 1 or 2, it is characterised in that：Each tower typical operation conditions are：
Lightness-removing column（T201）Tower top operating pressure scope is 30~195kPa；
First rectifying column（T202）Tower top operating pressure scope is 30~195kPa；
Second distillation column（T203）Tower top operating pressure scope is 160~950kPa；
Third distillation column（T204）Tower top operating pressure scope is 310~1500kPa.
9. according to the process described in claim 1 or 2, it is characterised in that：Each tower operating condition is：
Lightness-removing column（T201）Tower top operating pressure is 80~150kpa, and tower top operation temperature is 50~85 DEG C, tower reactor operation temperature
For 55~90 DEG C；
First rectifying column（T202）Tower top operating pressure is 80~180kpa, and tower top operation temperature is 50~90 DEG C, tower reactor operation
Temperature is 55~100 DEG C；
Second distillation column（T203）Tower top operating pressure is 160~500kPa, and tower top operation temperature is 70~130 DEG C, tower reactor behaviour
Make temperature as 75~140 DEG C；
Third distillation column（T204）Tower top operating pressure is 400~900kPa, and tower top operation temperature is 90~150 DEG C, and methanol carries
Evaporate side（L204）Tower reactor operation temperature is 135~180 DEG C；Ethyl alcohol rectifying side（R204）Tower reactor operation temperature is 110~160 DEG C.
10. a kind of device of four towers triple effect methanol rectification energy saving technique, it is characterised in that：Mainly include lightness-removing column（T201）,
One rectifying column（T202）, Second distillation column（T203）, third distillation column（T204）Four towers and connecting pipeline；
Raw material crude carbinol feed line is connected respectively with charging methanol preheater and charging waste water preheater cold side input port；
Charging methanol preheater and charging waste water preheater cold side outlet port are connected to lightness-removing column（T201）Middle part；Lightness-removing column（T201）
Tower top is connected with condenser of light component removal column, condenser of light component removal column condensate outlet and lightness-removing column（T201）Tower top connects, lightness-removing column condensation
The outlet of device fixed gas is connected with fixed gas discharge pipe line；Lightness-removing column（T201）Bottom uses a plurality of pipeline and first rectifying column
（T202）It is connected；
First rectifying column（T202）Tower top is connected with first rectifying column condenser, first rectifying column condenser condensate outlet respectively with
First rectifying column（T202）Tower top is connected with charging methanol preheater hot side entrance；First rectifying column（T202）Side line gas phase produces
Mouth and lightness-removing column（T201）Tower reactor is connected；First rectifying column（T202）Bottom respectively with first rectifying column reboiler tube-side inlet and
Second distillation column（T203）It is connected, the outlet of first rectifying column reboiler tube side is connected to first rectifying column（T202）Tower reactor；
Second distillation column（T203）Tower top is connected with first rectifying column reboiler shell side, and first rectifying column reboiler shell side lime set goes out
Mouth respectively with Second distillation column（T203）Tower top is connected with charging methanol preheater hot side entrance；Second distillation column（T203）Bottom
Respectively with Second distillation column reboiler tube-side inlet and third distillation column（T204）It is connected, the outlet of Second distillation column reboiler tube side
It is connected to Second distillation column（T203）Tower reactor；
Third distillation column（T204）Tower top is connected with Second distillation column reboiler shell side, and Second distillation column reboiler shell side lime set goes out
Mouth respectively with third distillation column（T204）Tower top is connected with charging methanol preheater hot side entrance；Third distillation column（T204）Methanol
Stripping side（L204）Bottom respectively with third distillation column methanol stripping side reboiler tube-side inlet and charging waste water preheater hot side
Entrance is connected, and reboiler tube side outlet in third distillation column methanol stripping side is connected to third distillation column（T204）Methanol stripping side
（L204）Tower reactor；Third distillation column（T204）Methanol stripping side（L204）Side take-off pipeline near charging is cooled down with fusel oil
Device hot side entrance connects；Third distillation column（T204）Ethyl alcohol rectifying side（R204）Bottom respectively with third distillation column ethyl alcohol rectifying side
Reboiler tube-side inlet is connected with ethyl alcohol cooler hot side entrance, third distillation column ethyl alcohol rectifying side reboiler tube side outlet connection
To third distillation column（T204）Ethyl alcohol rectifying side（R204）Tower reactor；
Charging methanol preheater hot side outlet is connected with methanol product cooler hot side entrance, methanol product cooler hot side outlet
It is connected with methanol product extraction pipeline；
Charging waste water preheater hot side outlet is connected with gaseous effluent cooler hot side entrance, and gaseous effluent cooler hot side outlet is respectively with taking off
Light tower（T201）Tower top is connected with discharge of wastewater pipeline；Fusel oil cooler hot side outlet connects with fusel oil product extraction pipeline
It connects；Ethyl alcohol cooler hot side outlet is connected with alcohol product extraction pipeline.
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