CN104496773A - Formaldehyde and dimethyl ether co-production technique - Google Patents
Formaldehyde and dimethyl ether co-production technique Download PDFInfo
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- CN104496773A CN104496773A CN201510034060.XA CN201510034060A CN104496773A CN 104496773 A CN104496773 A CN 104496773A CN 201510034060 A CN201510034060 A CN 201510034060A CN 104496773 A CN104496773 A CN 104496773A
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- formaldehyde
- dme
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/09—Preparation of ethers by dehydration of compounds containing hydroxy groups
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
- C07C45/37—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups
- C07C45/38—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups being a primary hydroxyl group
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a formaldehyde and dimethyl ether co-production technique. The formaldehyde and dimethyl ether co-production technique solves the problems of low tail gas utility ratio and complexity in production technique of an existing technique. According to the technical scheme, the formaldehyde and dimethyl ether co-production technique includes that firstly, filtering formaldehyde raw material; feeding the filtered formaldehyde to a formaldehyde reaction system and a dimethyl ether reaction system; reacting gas in the formaldehyde reaction system and the dimethyl ether reaction system to form a lot of combustible tail gas after reacting the reaction gas in the dimethyl ether reaction system and formaldehyde reaction system, gathering the combustible tail gas, using the gathered combustible tail gas as fuel of a boiler system, wherein the boiler system generates a lot of vapor to be supplied to the dimethyl ether reaction system, and condensed water formed after exchanging heat with the dimethyl ether reaction system is used as supplementary water for the boiler system. The formaldehyde and dimethyl ether co-production technique uses the technique properties of the formaldehyde and dimethyl ether, uses the waste heat and tail gas generated in the production process to meet the technique requirements thereof and solves the problem that the formaldehyde and dimethyl ether generate a lot of waste heat and waste water in the production process.
Description
Technical field
The present invention relates to formaldehyde and dme production field, particularly relate to a kind of formaldehyde, dme joint process.
Background technology
Formaldehyde is industrial important raw and processed materials, is widely used in the production of resin, plastics, leather, paper and fiber etc., plays an important role in the productive life of people.For improving the throughput of formaldehyde and utilizing its tail gas, existing technology has developed multiple production technique gradually on traditional formaldehyde production technology, comprises exhaust gas circulation process, low conversion without alcohol technique and flue gas recirculation technique etc.
One ton of formaldehyde products is often produced in Formaldehyde Production, by generation 37% tail gas, about more than 600 cube, containing hydrogen 18-20%, carbon monoxide, methane, oxygen each 0.5% in these tail gas, carbonic acid gas 5%, nitrogen 72-74%, water and trace formaldehyde, methyl alcohol etc., wherein about have about 20% combustible gas, its calorific value is at 2100-2300kj/m3.
And dme needs to consume relatively large water vapor in producing, need the steam of about 1.0Mpa200 DEG C that steam boiler produces to be sent in dimethyl ether production system in production process to use; Therefore the inflammable gas in formaldehyde reaction system and in dme reactive system and water vapour can use by Joint Replenishment, make both reactive systems form complementation.
Present people generally know that formaldehyde gas is harmful to, if production formaldehyde factory naturally discharges or burning and exhausting all can cause severe contamination to threaten to health of human body especially to environment.But containing the inflammable gas such as hydrogen, methane, carbon monoxide in formaldehyde tail gas, if can use is clean energy, Land use systems has varied but technique, and all more complicated investment is also larger.
Summary of the invention
For above-mentioned situation, for overcoming the defect of prior art, the object of the present invention is just to provide a kind of formaldehyde, dme joint process, and it is not high that object is to solve existing process tail gas utilization ratio, the problem of complex manufacturing.
Its technical scheme comprises the following steps:
Step one: crude carbinol raw material is filtered;
Step 2: the methyl alcohol after filtration enters formaldehyde reaction system and dme reactive system, enters methyl alcohol and air mixed in formaldehyde reaction system, and the methyl alcohol in PARA FORMALDEHYDE PRILLS(91,95) reactive system and air carry out preheating; Preheating is carried out to the methyl alcohol entered in dme reactive system;
Step 3: enter oxidation reactor after the air preheat in formaldehyde reaction system after preheating and carry out oxidizing reaction under the effect of catalyzer; Enter in dme reactive system and enter reactor after methyl alcohol preheating and carry out dehydration reaction;
Step 4: in formaldehyde reaction system, reacted gas enters absorption tower, water PARA FORMALDEHYDE PRILLS(91,95) gas is utilized to absorb, water-fast inflammable gas heats boiler systems as fuel, the water vapour produced after boiler systems heating carries out preheating to the methyl alcohol in dme reactive system, and the water of condensation that water vapour is formed in methyl alcohol heat-processed in dme reactive system returns boiler systems again; Carry out rectifying to gas reacted in dme reactive system, the product of rectifying is carrying out the laggard row gas-liquid separation of condensation, and wherein gas phase portion is washed by washing tower, is insoluble to the gas of washings as fuel boiler system after washing;
Step 5: the formaldehyde absorbent in PARA FORMALDEHYDE PRILLS(91,95) reactive system is collected; Collect methyl alcohol and dme in the non-condensable gas in dme reactive system after gas-liquid separation.
The present invention makes full use of the production technique characteristic of formaldehyde and dme, the used heat the two produced in process of production and waste gas utilization get up to provide self technique needs, greatly reduce traditional formaldehyde and dme and produce a large amount of used heat in process of production and to give up water problem.
Accompanying drawing explanation
Fig. 1 is schema of the present invention.
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in further detail.
As shown in Figure 1, formaldehyde, dme joint process, comprise the following steps:
Step one: crude carbinol raw material is filtered;
Step 2: the methyl alcohol after filtration enters formaldehyde reaction system and dme reactive system, enters methyl alcohol and air mixed in formaldehyde reaction system, and the methyl alcohol in PARA FORMALDEHYDE PRILLS(91,95) reactive system and air carry out preheating; Preheating is carried out to the methyl alcohol entered in dme reactive system;
Step 3: enter oxidation reactor after the air preheat in formaldehyde reaction system after preheating and carry out oxidizing reaction under the effect of catalyzer; Enter in dme reactive system and enter reactor after methyl alcohol preheating and carry out dehydration reaction;
Step 4: in formaldehyde reaction system, reacted gas enters absorption tower, water PARA FORMALDEHYDE PRILLS(91,95) gas is utilized to absorb, water-fast inflammable gas heats boiler systems as fuel, the water vapour produced after boiler systems heating carries out preheating to the methyl alcohol in dme reactive system, and the water of condensation that water vapour is formed in methyl alcohol heat-processed in dme reactive system returns boiler systems again; Carry out rectifying to gas reacted in dme reactive system, the product of rectifying is carrying out the laggard row gas-liquid separation of condensation, and wherein gas phase portion is washed by washing tower, is insoluble to the gas of washings as fuel boiler system after washing;
Step 5: the formaldehyde absorbent in PARA FORMALDEHYDE PRILLS(91,95) reactive system is collected; Collect methyl alcohol and dme in the non-condensable gas in dme reactive system after gas-liquid separation.
Said step one, methanol feedstock is stored in methyl alcohol tank field, and in methanol tank, methyl alcohol is sent into methyl alcohol header tank through methanol pump by methyl alcohol, and the methyl alcohol through methyl alcohol header tank enters methyl alcohol strainer.
Said step 2, filter complete methyl alcohol and send into evaporator tower, said air sends into evaporator tower through gas blower again after air filter filters, the mass ratio entering oxygen in evaporator tower and methyl alcohol is 0.38-0.42, preheating is carried out to the methyl alcohol and air that enter evaporator tower, makes its temperature be in 105-120 DEG C; The methyl alcohol entered after filtering in dme reactive system flows through liquid waste cooler, methanol evaporator, methanol distillation column and gas heat exchanger successively after methyl alcohol dashpot, methanol distillation column is heated by water vapour, water vapour is supplied by boiler systems, the water of condensation that water vapour is formed through heat exchange cooling enters boiler again through boiler circulating line, forming reactions gas in the dehydration reaction of methyl alcohol, reaction gas carries the large calorimetric formed in dehydration reaction, reaction gas flows through methanol evaporator through pipeline, heats the methyl alcohol in methanol evaporator.
Said step 3, gas in formaldehyde reaction system after preheating connects secondary filter through spark arrester after preheating, gas after preheating is filtered again, three vigour after filtration enter formaldehyde reaction device, said catalyzer is electrolytic silver, under 630-660 DEG C of condition, catalyzed oxidation and dehydrogenation reaction is there is in methyl alcohol under the effect of catalyzer, the water vapour carrying large calorimetric is produced in reaction process, water vapour sends into three vigour that evaporator tower forms methanol-air-water vapour, and the heat utilizing water vapour to carry realizes methyl alcohol and preheating of air; Enter dimethyl ether reactor after entering the methyl alcohol preheating in dme reactive system, and at the temperature of 340-380 DEG C, dehydration reaction occurs.
Said absorption tower comprises the first absorption tower and the second absorption tower of series connection, in formaldehyde reaction system, first reacted gas send into the first absorption tower, do not entered second absorption tower by the gas that the first absorption tower absorbs, form rare formaldehyde solution after liquid-absorbent formaldehyde in second absorption tower, rare formaldehyde solution sends into the first absorption tower through recycle pump and second absorption tower tower top supplements its absorption liquid; In dme reactive system, reacted gas sends into dme distillation tower, rectifying tower top is provided with evaporating water cooled device, reacted gas is cooled by evaporating water cooled device, cooled dme enters dme backflash, dme backflash carries out gas-liquid separation to dme, and the gas phase portion that separation obtains enters washing tower and carries out washing absorption.
Send after the formaldehyde absorbent cooling in the first absorption tower into formaldehyde solution storer; Reflux to the dme in dme backflash, a part returns dme rectifying tower after pump pressurizes and measures, and another part sends into dme product storer after metering.
The present invention makes full use of the production technique characteristic of formaldehyde and dme, the used heat the two produced in process of production and waste gas utilization get up to provide self technique needs, greatly reduce traditional formaldehyde and dme and produce a large amount of used heat in process of production and to give up water problem.
Claims (6)
1. formaldehyde, dme joint process, comprises the following steps:
Step one: crude carbinol raw material is filtered;
Step 2: the methyl alcohol after filtration enters formaldehyde reaction system and dme reactive system, enters methyl alcohol and air mixed in formaldehyde reaction system, and the methyl alcohol in PARA FORMALDEHYDE PRILLS(91,95) reactive system and air carry out preheating; Preheating is carried out to the methyl alcohol entered in dme reactive system;
Step 3: enter oxidation reactor after the air preheat in formaldehyde reaction system after preheating and carry out oxidizing reaction under the effect of catalyzer; Enter in dme reactive system and enter reactor after methyl alcohol preheating and carry out dehydration reaction;
Step 4: in formaldehyde reaction system, reacted gas enters absorption tower, water PARA FORMALDEHYDE PRILLS(91,95) gas is utilized to absorb, water-fast inflammable gas heats boiler systems as fuel, the water vapour produced after boiler systems heating carries out preheating to the methyl alcohol in dme reactive system, and the water of condensation that water vapour is formed in methyl alcohol heat-processed in dme reactive system returns boiler systems again; Carry out rectifying to gas reacted in dme reactive system, the product of rectifying is carrying out the laggard row gas-liquid separation of condensation, and wherein gas phase portion is washed by washing tower, is insoluble to the gas of washings as fuel boiler system after washing;
Step 5: the formaldehyde absorbent in PARA FORMALDEHYDE PRILLS(91,95) reactive system is collected; Collect methyl alcohol and dme in the non-condensable gas in dme reactive system after gas-liquid separation.
2. formaldehyde according to claim 1, dme joint process, said step one, methyl alcohol is sent into methyl alcohol header tank through methanol pump by methanol feedstock, and the methyl alcohol through methyl alcohol header tank enters methyl alcohol strainer.
3. formaldehyde according to claim 1, dme joint process, said step 2, filter complete methyl alcohol and send into evaporator tower, said air sends into evaporator tower through gas blower again after air filter filters, the mass ratio entering oxygen in evaporator tower and methyl alcohol is 0.38-0.42, preheating is carried out to the methyl alcohol and air that enter evaporator tower, makes its temperature be in 105-120 DEG C; The methyl alcohol entered after filtering in dme reactive system flows through liquid waste cooler, methanol evaporator, methanol distillation column and gas heat exchanger successively after methyl alcohol dashpot, methanol distillation column is heated by water vapour, water vapour is supplied by boiler systems, the water of condensation that water vapour is formed through heat exchange cooling enters boiler again through boiler circulating line, forming reactions gas in the dehydration reaction of methyl alcohol, reaction gas carries the large calorimetric formed in dehydration reaction, reaction gas flows through methanol evaporator through pipeline, heats the methyl alcohol in methanol evaporator.
4. formaldehyde according to claim 1, dme joint process, said step 3, gas in formaldehyde reaction system after preheating connects secondary filter through spark arrester after preheating, gas after preheating is filtered again, three vigour after filtration enter formaldehyde reaction device, said catalyzer is electrolytic silver, under 630-660 DEG C of condition, catalyzed oxidation and dehydrogenation reaction is there is in methyl alcohol under the effect of catalyzer, the water vapour carrying large calorimetric is produced in reaction process, water vapour sends into three vigour that evaporator tower forms methanol-air-water vapour, the heat utilizing water vapour to carry realizes methyl alcohol and preheating of air, enter dimethyl ether reactor after entering the methyl alcohol preheating in dme reactive system, and at the temperature of 340-380 DEG C, dehydration reaction occurs.
5. formaldehyde according to claim 1, dme joint process, it is characterized in that, said absorption tower comprises the first absorption tower and the second absorption tower of series connection, in formaldehyde reaction system, first reacted gas send into the first absorption tower, do not entered second absorption tower by the gas that the first absorption tower absorbs, form rare formaldehyde solution after liquid-absorbent formaldehyde in second absorption tower, rare formaldehyde solution sends into the first absorption tower through recycle pump and second absorption tower tower top supplements its absorption liquid; In dme reactive system, reacted gas sends into dme distillation tower, rectifying tower top is provided with evaporating water cooled device, reacted gas is cooled by evaporating water cooled device, cooled dme enters dme backflash, dme backflash carries out gas-liquid separation to dme, and the gas phase portion that separation obtains enters washing tower and carries out washing absorption.
6. formaldehyde according to claim 5, dme joint process, is characterized in that, sends after the formaldehyde absorbent cooling in the first absorption tower into formaldehyde solution storer; Reflux to the dme in dme backflash, a part returns dme rectifying tower after pump pressurizes and measures, and another part sends into dme product storer after metering.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510034060.XA CN104496773A (en) | 2015-01-23 | 2015-01-23 | Formaldehyde and dimethyl ether co-production technique |
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| CN201510034060.XA CN104496773A (en) | 2015-01-23 | 2015-01-23 | Formaldehyde and dimethyl ether co-production technique |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107778272A (en) * | 2017-11-02 | 2018-03-09 | 王建玲 | A kind of method and apparatus that hemiacetal is produced using alcohol dehydrogenase |
| CN107881523A (en) * | 2017-10-27 | 2018-04-06 | 中石化宁波工程有限公司 | A kind of process for making hydrogen containing carbon pastes |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6403841B1 (en) * | 1999-09-22 | 2002-06-11 | Japan Science And Technology Corporation | Process for preparing partial oxidates of lower alcohols |
| CN101195561A (en) * | 2007-12-26 | 2008-06-11 | 成都天成碳一化工有限公司 | Method for producing dimethyl ether with methanol gas-phase dehydration |
| CN101274881A (en) * | 2008-05-19 | 2008-10-01 | 杨奇申 | Energy-saving method for producing dimethy ether by boiler with residual heat |
| CN102320942A (en) * | 2011-06-14 | 2012-01-18 | 田宝峰 | Production process and device of formaldehyde |
-
2015
- 2015-01-23 CN CN201510034060.XA patent/CN104496773A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6403841B1 (en) * | 1999-09-22 | 2002-06-11 | Japan Science And Technology Corporation | Process for preparing partial oxidates of lower alcohols |
| CN101195561A (en) * | 2007-12-26 | 2008-06-11 | 成都天成碳一化工有限公司 | Method for producing dimethyl ether with methanol gas-phase dehydration |
| CN101274881A (en) * | 2008-05-19 | 2008-10-01 | 杨奇申 | Energy-saving method for producing dimethy ether by boiler with residual heat |
| CN102320942A (en) * | 2011-06-14 | 2012-01-18 | 田宝峰 | Production process and device of formaldehyde |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107881523A (en) * | 2017-10-27 | 2018-04-06 | 中石化宁波工程有限公司 | A kind of process for making hydrogen containing carbon pastes |
| CN107881523B (en) * | 2017-10-27 | 2020-02-11 | 中石化宁波工程有限公司 | Carbon-containing slurry hydrogen production process |
| CN107778272A (en) * | 2017-11-02 | 2018-03-09 | 王建玲 | A kind of method and apparatus that hemiacetal is produced using alcohol dehydrogenase |
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Application publication date: 20150408 |