CN1326918A - Producing equipment for formaldehyde and its completed production process - Google Patents
Producing equipment for formaldehyde and its completed production processInfo
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- CN1326918A CN1326918A CN 01120189 CN01120189A CN1326918A CN 1326918 A CN1326918 A CN 1326918A CN 01120189 CN01120189 CN 01120189 CN 01120189 A CN01120189 A CN 01120189A CN 1326918 A CN1326918 A CN 1326918A
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Abstract
The formaldehyde producing equipment includes compounding vapor drum, technological vapor drum, methanol vapor drum, vapor washing tower, hot pressing pump, rectangular reactor in horizontal comb structure with built-in cooler. The material gases from the compounding vapor drum and the methanol vapor drum are washed in vapor washing tower, passed through the hot pressing pump and made to flow to the reactor to produce formaldehyde. The present invention has less pollution to silver catalyst, low material consumption and power consumption, adaptive control, improved heat transfer condition and other advantages.
Description
The present invention relates to a kind of production unit of formaldehyde and the production technique that this equipment is finished thereof.
Produced in the past in the technology of formaldehyde adopt air blasted in the methyl alcohol of heating obtain methyl alcohol and Air mixing gas, again water vapour is methylated with Air mixing gas in, finish the blending process of unstripped gas.These unstripped gases that prepare are transported in the superheater and heat, again by entering after the filter process in the reactor, reaction generates formaldehyde under the effect of silver catalyst, enter the first grade absorption tower in the reactor again after the cooling of cooling zone in reactor, these formaldehyde gases promptly become finished product after being absorbed by one-level, not absorbent product again after two-level absorption tower, three grades of absorption towers etc. absorb nonabsorbable gas promptly with exhaust emissions.Because air blasts and needs electric energy in the methyl alcohol, needs electric energy in the gas delivery process, gas needs electric energy during by strainer, thereby consumes a large amount of electric energy.Unstripped gas only promptly enters in the reactor through simple filtration, because the unstripped gas purity is not high, with catalyzer contact stain catalyzer, causes working condition to worsen with the cycle of operation and shortens, and influences the output and the unit consumption of formaldehyde.And with the increase of impurity, filter mesh reduces in the filtration procedure, and the replacing filtration medium that must stop behind the impurity obstruction filter mesh influences formaldehyde output.The technology of Yi Qian production formaldehyde and equipment thereof the output and the quality that influence formaldehyde consumes a large amount of electric energy in a word, influences the economic benefit of producer.
The present invention overcomes exactly and goes up shortcoming, and a kind of production unit of the formaldehyde that can effectively increase driving time, save energy, reduction unit consumption and the technology that this equipment is finished thereof are provided.
For finishing first purpose of the present invention, technical solution of the present invention is: a kind of production unit of formaldehyde, it comprises: batching water vapor gas bag, process water steam gas bag, methanol steam gas bag, steaming tower, air cleaning unit, constant volume gas blower, recycle pump, superheater, hot pressing pump, reactor, multistage absorption tower.Have the import of raw material soft water, raw material soft loop exit and import and vapour outlet on the batching water vapor gas bag; Have the import of material benzenemethanol liquid, loop exit and the import and the methanol gas outlet of material benzenemethanol liquid on the methanol steam gas bag; Have the import of raw material soft, raw material soft loop exit and import and vapour outlet on the process water steam gas bag, vapour outlet is by the heating medium import of each superheater of pipe connection; The steaming tower is divided into batching steaming tower and methanol steam washing tower, it is to be with, the tubular tower of lower cover, condenser by screen support fixed packing layer and packing layer upper end is arranged in the tower body, on the tower body at condenser place, have advancing of cooling medium, outlet, on the tower body of screen support lower end, have raw material gas inlet, on the tower body between condenser and packing layer, have pneumatic outlet, the raw material gas inlet of steaming tower of wherein preparing burden is connected by the vapour outlet of pipeline with batching water vapor gas bag, pneumatic outlet is connected by the center nozzle of pipeline with the hot pressing pump, the raw material gas inlet of methanol steam washing tower is connected with the methanol gas outlet of methanol steam gas bag by pipeline, pneumatic outlet is connected with the gas feed of superheater by pipeline, and the pneumatic outlet by superheater is connected with the peripheral spout of hot pressing pump by pipeline again; There are two concentric orifice the upper end of hot pressing pump: center nozzle and peripheral spout, have the import of raw air on the side, and there is a diffuser tube centre, and the lower end is a mixed gas outlet; Raw air is introduced the raw air import of hot pressing pump again by being introduced in the superheater by the constant volume gas blower behind the air cleaning unit by superheater; The mixed gas outlet of hot pressing pump is by the unstripped gas import of pipe connection superheater, again by the unstripped gas outlet of the superheater cap by the pipe connection reactor; Reactor is a rectangle, reactor comprises cap, by catalyst basket fixed catalyst layer, the chilling tubulation is distinguished, two districts, three districts and first grade absorption tower, reactor cap and reactor body wall topmost is fixed together by flange seal, the catalyst basket bottom of cap lower end is porous card or segmentation porous card, the upper end of catalyst basket is fixed on the flange connections of cap and main wall, there is catalyst layer on catalyst basket upper berth, catalyst basket lower end is the chilling tubulation district of horizontal positioned tubulation, the chilling tubulation is divided into a district, two districts, three districts, the tubulation in chilling tubulation one district is connected with the sidewall of reactor end socket, and on end socket, having batching with soft circulation import and outlet, this import and outlet are connected by recycle pump by pipeline with import with raw material soft loop exit on the water vapor gas bag of preparing burden; The tubulation in chilling tubulation two districts also is connected with herein sidewall end socket, and has technology with soft circulation import and outlet on end socket, and the raw material soft loop exit of this import and outlet and process water steam gas bag and import are by pipe connection; The tubulation in chilling tubulation three districts also links to each other with the sidewall end socket, and has the circulation import and the outlet of methanol liquid on end socket, and the loop exit of the methanol liquid on this import and outlet and the methanol steam gas bag and import are by pipe connection; Lower end, chilling tubulation district is a first grade absorption tower, there is a circulating liquid sparger upper end of first grade absorption tower, the liquid distributor lower end is built-in water cooler, the lower end is by screen support fixed packing layer again, outlet and the circulation fluid outlet of lower end for connecting the multistage absorption tower again, the circulation fluid outlet connects the circulating liquid sparger by pipeline by recycle pump, and the outlet of a formaldehyde finished product is arranged on the pipeline that connects circulation fluid outlet and circulating liquid sparger.
The production unit of a kind of formaldehyde of the present invention, wherein the porous card or the segmentation porous card of the catalyst basket of reactor bottom are arc.
The production unit of a kind of formaldehyde of the present invention, wherein reactor chilling tubulation district respectively distinguishes tubulation all arc-shaped bend, one district promptly matches near the tubulation crooked radian and the card crooked radian of porous card near the chilling tubulation district of catalyst basket, can make tubulation and card spacing minimum herein like this, increase the chilling effect, reduce side reaction.Crooked tubulation can effectively absorb the stress that is produced by the temperature difference, can prolong equipment life.
Air cleaning unit described in the production unit of formaldehyde of the present invention is an air scrubber, it is the tower that upper cover is arranged, have in the tower body by screen support fixed packing layer, the fog blocker of the liquid distributor of packing layer upper end and liquid distributor upper end, have the raw air import on the tower body of lower end, the emptied of air import, the circulating cleaning solution outlet, have the outlet of raw air on the tower body of upper end, circulating cleaning solution exports by recycle pump by the pipe connection liquid distributor, on this pipeline, have one to replenish the washings inlet, the raw air outlet is connected the import of superheater by the constant volume gas blower by pipeline, one outlet is arranged on this pipeline, and this outlet is by the emptied of air import of pipe connection air scrubber.
For finishing another object of the present invention, technical solution of the present invention is: a kind of Formaldehyde Production technology of finishing by the production unit of above-mentioned formaldehyde, and it may further comprise the steps:
1. highly purified raw material soft water is sent in the batching water vapor gas bag, send into chilling tubulation one district by batching water vapor gas bag by recycle pump again, enter batching water vapor gas bag internal recycle by reaction heat after to its heating, produce a large amount of high-temperature high-pressure steams in the batching water vapor gas bag, these water vapors enter in the moistening packing layer of steaming tower and wash cleaning, the center nozzle that the major part of the raw water steam after the washing cleaning enters the hot pressing pump is ejected in the hot pressing pump, after the washings that forms cleaning after the condenser condenses of raw water steam by steaming tower top of small portion cleaning is back in the packing layer washing raw water steam and filler, carries impurity secretly and be back in the batching water vapor gas bag and circulate;
2. raw material soft water is sent in the process water steam gas bag, flow to chilling tubulation two districts of reactor, by reaction heat to its heating after enter process water steam gas bag internal recycle, produce a large amount of high-temperature high-pressure steams in the process water steam gas bag, these water vapors enter in all superheaters the heating medium as superheater;
3. methanol feedstock is sent in the methanol steam gas bag, flow to chilling tubulation three districts of reactor, by reaction heat to its heating after get back to methanol steam gas bag internal recycle, produce a large amount of High Temperature High Pressure methanol gas in the methanol steam gas bag, these methanol gas enter in the moistening packing layer of steaming tower and wash cleaning, material benzenemethanol gas major part after the washing cleaning enter carry out in the superheater overheated, the peripheral spout that enters the hot pressing pump then is ejected in the hot pressing pump, the washings that the material benzenemethanol gas of small portion cleaning forms cleaning by the condenser condenses on steaming tower top is back in the packing layer after the washing methanol gas and filler, carries impurity secretly and is back in the methanol steam gas bag and circulates;
4. raw air is introduced in the superheater by the constant volume gas blower by refining plant, the raw air import that enters the hot pressing pump after the heating again;
5. in the hot pressing pump, have by the water vapor of center nozzle high-velocity jet, have, the raw air that is entered by air intlet is arranged by the methyl alcohol of peripheral spout high-velocity jet, three kinds of unstripped gases are taken out band and are mixed the tail end that afterwards flows to the hot pressing pump by the diffuser tube of hot pressing pump, flow to superheater by mixed gas outlet.
6. through the cap of three kinds of mixing raw material gas flows of superheater superheated reactor, the catalyst layer that enters reactor that flows downward carries out oxidizing reaction generation formaldehyde gas, formaldehyde gas flows to the chilling tubulation district of reactor, by chilling tubulation one district, chilling tubulation two districts, after cooling off successively, chilling tubulation three districts enter the first grade absorption tower of reactor, in first grade absorption tower, entered condensation absorption formation formaldehyde liquid in the packing layer again after the built-in water cooler cooling, the absorption that circulates of most of formaldehyde liquid, increase the liquid part as the finished product extraction, nonabsorbable formaldehyde gas is absorbed the back recovering liquid by the multistage absorption tower again and returns first grade absorption tower bottom, exhaust emissions.
In the above-mentioned described Formaldehyde Production technology, the process that its raw air enters the hot pressing pump also can be: raw air enters the interior washing cleaning of the moistening packing layer back of air scrubber by heating in the constant volume gas blower introducing superheater, the air of emptying then still is back to the air washing tower bottom and participates in washing process, washings in the packing layer is the liquid distributor liquid of ejection downwards, this liquid is supplied with by circulating liquid, insufficient part or the liquid when just having started equipment derive from additional washings, are entered in the hot pressing pump by the air intlet of hot pressing pump by the superheater superheated air that comes out again.
Owing to adopted such scheme, the present invention has the following advantages compared with prior art:
1. the present invention adopts the finished product formaldehyde gas heat that carries to be passed to successively chilling tubulation one district, chilling tubulation two districts, chilling tubulation three districts in process of cooling, so that batching water, process water and methanol solution obtain heat and form high temperature and high pressure gas, utilize this pressure, can be with the equipment conveying rearwards of these gases, make production used heat obtain the high-performance utilization, saved the spent electric energy of transferring raw material gas; And the formaldehyde output of producing is many more, and the heat of reaction is big more, otherwise then the little heat of the output of formaldehyde is also few, has been issued to the balance of heat production and heat dissipation in various processing condition, produces adaptive control effect.
2. the present invention can and prepare burden water separately with process water like this because process water steam gas bag can independently supply water with batching water vapor gas bag, reduces raw material water cost.
3. the present invention has adopted more reliable, the scavenging process more fully of more former filter method, purification steaming tower with batching water vapor and methanol gas, catalyzer can keep suitable clean conditions aborning, because electrolytic silver has continuous growth aborning and upgrades the effect of active center, the speed that the performance of catalyzer improves can be higher than the speed of contamination of raw material in this purification style, thereby the conversion performance that makes catalyzer keeps permanent rising and stable, reduce the driving number of times, reduce unit consumption and energy consumption.Air cleaning unit adopts air scrubber, makes air clean more, reduces the opportunities for contamination of silver.
4. reactor of the present invention adopts the horizontal row tubular construction, make the useless pot of original fire tube change over high performance water tube donkey structure, can effectively improve the liquid in pipe flow velocity, improve heat transfer condition, solve the structure deteriorate problem that the easy discharge chamber of former used equipment destroys and stress causes.Utilize arc tubulation structure, tubulation can be absorbed easily voluntarily, prevented the stress corrosion destruction of material and the structure deteriorate that stress causes because the dimensional variations that temperature variation is brought makes it not produce the stress concentration phenomenon.
5. the present invention adopts and flows absorption, built-in water cooler, and its treatment capacity is big, does not have general tower point, and the tower air speed can so its tower diameter can reduce, have been saved investment more than 4m/s, reduce than the traditional technology internal circulating load, thereby saved electric energy.
6. reactor adopts rectangular configuration, broken through circular configuration to the restriction of scale (because of catalyzer for manually mating formation, the diameter of circular reactor is subjected to the restriction of arm length), rectangular configuration can be no more than under the limit operation size condition, choose rectangle size dimension on one side, and the other side rectangle length of side can be chosen arbitrarily, thereby can enlarge the device fabrication scale greatly.
7. the arc of the bending curvature of chilling tubulation of the present invention and catalyst basket bottom matches, and has reduced the idle space of reactor quench zone tubulation and catalyst layer, has improved the condition of chilling, and the side reaction that helps to reduce under the catalyst layer takes place.
Below in conjunction with the drawings and specific embodiments in detail the present invention is described in detail:
Fig. 1 is a process flow sheet of the present invention;
Fig. 2 is the cross-sectional view of reactor in the present device;
Fig. 3 is the cross-sectional view of steam purifier in the present device;
Fig. 4 is the cross-sectional view of air purifier in the present device;
Fig. 5 is the cross-sectional view of hot pressing pump in the present device;
As shown in Figure 1, the equipment of Formaldehyde Production of the present invention comprises batching water vapor gas bag 2, process water steam gas bag 1, methanol steam gas bag 3, steaming tower 3 and 5, air scrubber 9, constant volume gas blower 12, recycle pump 18,10,17, hot pressing pump 8, superheater 6,7,11, rectangular reactor 16, two-level absorption tower 15, three grades of absorption towers 14 and level Four absorption towers 13.Carry out producing the raw water steam after the heating cycle in the highly purified raw material soft water input batching water vapor gas bag 2, the raw water steam sprays in the hot pressing pump 8 after steaming tower 3 washing cleanings; Carry out producing material benzenemethanol gas after the heating cycle in the methanol liquid input methanol steam gas bag 4, it is overheated that methanol gas enters in the superheater 6 after steaming tower 5 washing cleanings, and superheated material benzenemethanol gas sprays in the hot pressing pump 8; Washing cleaning back is blasted in the hot pressing pump 8 by constant volume gas blower 12 in the air admission air scrubber 9; Three kinds of unstripped gases are taken out the band mixing in hot pressing pump 8 after, in the diffuser tube of hot pressing pump 8, constantly lower flow and form the high pressure area at the tail end of hot pressing pump, three kinds of raw materials since pressure current to superheater 7 internal heating, flow to then in the cap of reactor 16, enter catalyst layer downwards and carry out oxidizing reaction generation formaldehyde gas, formaldehyde gas enters first grade absorption tower after chilling tubulation one district, two districts, the cooling of three districts.In first grade absorption tower, entered cooling and absorbing formation formaldehyde liquid in the packing layer again after the built-in water cooler cooling, the absorption that circulates of most of formaldehyde liquid, increase the liquid part as the product extraction, nonabsorbable formaldehyde gas is absorbed the back recovering liquid by absorption towers such as secondary, three grades, level Four 15,14,13 again and returns first grade absorption tower bottom, exhaust emissions.
As shown in Figure 2, the cap 19 of rectangular reactor passes through flange 20 sealing and fixing together with main wall, catalyst basket 21 bottoms of cap 19 lower ends are arc porous card, the upper end of catalyst basket 21 is fixed on flange 20 junctions of cap 19 and main wall, be covered with catalyst layer on the catalyst basket 21, chilling tubulation one district of catalyst basket lower end, two districts, the arc-shaped bend of the arc-shaped bend of the tubulation in three districts and porous card matches, the tubulation 22 in tubulation one district is connected with sidewall end socket 23, the tubulation 24 in tubulation two districts is connected with sidewall end socket 25, and the tubulation 26 in tubulation three districts is connected with sidewall end socket 27; Circulation fluid outlet 35 is connected with liquid distributor 28 by recycle pump 17 by pipeline, have formaldehyde product outlet 34 on this pipeline, the tubulation 29 of built-in condenser is connected with tower side wall end socket 30, cooling medium flows into from import 31, flow out from exporting 38, packing layer 32 is a structured filling material layer, to reach the purpose of efficient absorption, the gases such as formaldehyde that do not have to absorb lead to secondary by outlet 33, three grades, level Four absorption tower 15,14,13, formaldehyde liquid after the absorption draws back first grade absorption tower by inlet 36, the nonabsorbable non-condensable gases in level Four absorption tower is discharged as tail gas, and 37 is the sewage draining exit of reactor.
As shown in Figure 3, have the import 39 of gas on the end socket of steaming tower lower end, inside has by screen support 40 fixed packing layers 41, packing layer 41 is a structured filling material layer, the upper end of packing layer 41 is a condenser, condenser is by last, lower tubesheet 45 and 42 and tubulation between the two 43 form, tubulation 43 is evenly arranged between tube sheet 45 and 42, tubulation 43 preferably with rounded projections arranged between tube sheet 45 and 42, cooling medium is full of between two tube sheets and tubulation, raw material steam for being cooled in the tubulation, in the condenser lower end, have pneumatic outlet 48 on the body wall of the washing tower of the upper end of packing layer, the import 44 that has cooling medium on the body wall at condenser position is the noncondensable gas relief outlet with outlet 47,46.
As shown in Figure 4, air scrubber is to have the tubular tower of upper cover, have in the tower body by the liquid distributor 55 of screen support 53 fixed packing layers 54, packing layer upper end and the fog blocker 56 of liquid distributor upper end, have outlet 50 of raw air import 52 circulating cleaning solutions and emptied of air import 58 in the bottom of tower, have air 57 on the upper cover.Circulating cleaning solution outlet 50 by recycle pump 51 by pipe connection to liquid distributor, have one to replenish washings and enter the mouth 49 on this pipeline.
As shown in Figure 5, two concentric orifice are arranged on the hot pressing pump: center nozzle 62 and peripheral spout 61, have air intlet 63 on the sidewall, a diffuser tube 60 is arranged in the lower end of spout and import, then be the outlet 59 of mixed gas bottom.
Claims (8)
1. Formaldehyde Production equipment, it comprises reactor, multistage absorption tower, air cleaning unit, superheater, constant volume gas blower, recycle pump, it is characterized in that it also comprises batching water vapor gas bag, process water steam gas bag, methanol steam gas bag, steaming tower and hot pressing pump; Have the import of raw material soft water, raw material soft loop exit and import and steam outlet on the batching water vapor gas bag; Have the import of material benzenemethanol liquid, loop exit and the import and the methanol gas outlet of material benzenemethanol liquid on the methanol steam gas bag; Have the import of raw material soft, raw material soft loop exit and import and steam outlet on the process water steam gas bag, steam outlet is by the heating medium import of each superheater of pipe connection; The steaming tower is divided into batching steaming tower and methanol steam washing tower, it is to be with, the tubular tower of lower cover, condenser by screen support fixed packing layer and packing layer upper end is arranged in the tower body, on the tower body at condenser place, have advancing of cooling medium, outlet, on the tower body of screen support lower end, have raw material gas inlet, on the tower body between condenser and packing layer, have pneumatic outlet, the raw material gas inlet of steaming tower of wherein preparing burden is connected by the steam outlet of pipeline with batching water vapor gas bag, pneumatic outlet is connected by the center nozzle of pipeline with the hot pressing pump, the raw material gas inlet of methanol steam washing tower is connected by the pneumatic outlet of pipeline with the methanol steam gas bag, pneumatic outlet is connected with the gas feed of superheater by pipeline, and the pneumatic outlet by superheater is connected with the peripheral spout of hot pressing pump by pipeline again; There are two concentric orifice the upper end of hot pressing pump: center nozzle and peripheral spout, have the import of raw air on the side, and there is a diffuser tube centre, and the lower end is a mixed gas outlet; Raw air is by being introduced in the superheater by the constant volume gas blower behind the air cleaning unit, again by the outlet of the superheater raw air import by pipe connection hot pressing pump; The mixed gas outlet of hot pressing pump is exported the cap of ligation device again by the unstripped gas import of pipe connection superheater by the unstripped gas of superheater; Reactor is a rectangle, reactor comprises cap, by catalyst basket fixed catalyst layer, the chilling tubulation is distinguished, two districts, three districts and first grade absorption tower, reactor cap and reactor body wall topmost is fixed together by flange seal, the catalyst basket bottom of cap lower end is porous card or segmentation porous card, the upper end of catalyst basket is fixed on the flange connections of cap and main wall, there is catalyst layer on catalyst basket upper berth, catalyst basket lower end is the chilling tubulation district of horizontal positioned tubulation, the chilling tubulation is divided into a district, two districts, three districts, the tubulation in chilling tubulation one district is connected with the end socket of sidewall of reactor, and on end socket, having batching with soft circulation import and outlet, this import and outlet are connected by recycle pump by pipeline with import with raw material soft loop exit on the water vapor gas bag of preparing burden; The tubulation in chilling tubulation two districts also is connected with herein sidewall end socket, and has technology with soft circulation import and outlet on end socket, and raw material soft loop exit on this import and outlet and the process water steam gas bag and import are by pipe connection; The tubulation in chilling tubulation three districts also is connected with sidewall end socket herein, and has the circulation import and the outlet of methanol liquid on end socket, and the loop exit of the methanol liquid of this import and outlet and methanol steam gas bag and import are by pipe connection; Lower end, chilling tubulation district is a first grade absorption tower, there is a circulating liquid sparger upper end of first grade absorption tower, the liquid distributor lower end is a built-in water cooler, the lower end is by screen support fixed packing layer again, outlet and the circulation fluid outlet of lower end for connecting the multistage absorption tower again, the circulation fluid outlet connects the circulating liquid sparger by pipeline by recycle pump, and the outlet of a formaldehyde finished product is arranged on the pipeline that connects circulation fluid outlet and circulating liquid sparger.
2. the production unit of formaldehyde according to claim 1, it is characterized in that described air cleaning unit is an air scrubber, it is the tower that upper cover is arranged, have in the tower body by the liquid distributor of screen support fixed packing layer, packing layer upper end and the fog blocker of liquid distributor upper end, have raw air import, emptied of air import and circulating cleaning solution outlet on the tower body of lower end, have the outlet of raw air on the upper cover, the circulating cleaning solution outlet by the pipe connection liquid distributor, has one to replenish the washings inlet by recycle pump on this pipeline; The raw air outlet has an outlet by the import of pipeline by constant volume gas blower connection superheater on this pipeline, this outlet is by the emptied of air import of pipe connection air scrubber.
3. the production unit of formaldehyde according to claim 1, the packing layer that it is characterized in that described steaming tower and reactor is a structured filling material layer.
4. the production unit of formaldehyde according to claim 1 is characterized in that the porous card or the segmentation porous card of catalyst basket bottom is arc.
5. the production unit of formaldehyde according to claim 1, the chilling tubulation district that it is characterized in that described reactor respectively distinguishes tubulation arc-shaped bend, and a district promptly matches near the tubulation crooked radian and the card crooked radian of porous card near the chilling tubulation district of catalyst basket.
6. the production unit of formaldehyde according to claim 1, the condenser that it is characterized in that described steaming tower is made up of upper and lower tube sheet (45) and (42) and the tubulation between the two (43) thereof, tubulation (43) is evenly arranged between tube sheet (45) and (43), cooling medium is full of between two tube sheets and tubulation, the raw material steam for being cooled in the tubulation.
7. the Formaldehyde Production technology finished of the production unit of formaldehyde according to claim 1, it is characterized in that: it may further comprise the steps:
(1) highly purified raw material soft water is sent in the described batching water vapor gas bag, send into chilling tubulation one district by batching water vapor gas bag by recycle pump again, enter batching water vapor gas bag internal recycle by reaction heat after to its heating, produce a large amount of high-temperature high-pressure steams in the batching water vapor gas bag, these water vapors enter in the moistening packing layer of steaming tower and wash cleaning, the center nozzle that the major part of the raw water steam after the washing cleaning enters the hot pressing pump is ejected in the hot pressing pump, form clean washings after the condenser condenses of raw water steam by steaming tower top of small portion cleaning and be back in the packing layer behind the washing raw water steam and filler, carry impurity secretly and be back in the batching water vapor gas bag and circulate;
(2) raw material soft water is sent in the process water steam gas bag, flow to chilling tubulation two districts of reactor, by reaction heat to its heating after enter process water steam gas bag internal recycle, produce a large amount of high temperature, high-pressure water vapor in the process water steam gas bag, these water vapors enter in institute's having heaters as heating medium;
(3) methanol feedstock is sent in the methanol steam gas bag, flow to chilling tubulation three districts of reactor, by reaction heat to its heating after get back to methanol steam gas bag internal recycle, produce a large amount of high temperature in the methanol steam gas bag, the high pressure methanol gas, this methanol gas enters in the moistening packing layer of steaming tower and washs cleaning, material benzenemethanol gas major part after the washing cleaning enter carry out in the superheater overheated, enter then in the peripheral spout of hot pressing pump, be ejected in the hot pressing pump, the washings that the material benzenemethanol gas of small portion cleaning forms cleaning by the condenser condenses on steaming tower top is back to be carried impurity secretly and is back in the methanol steam gas bag and circulates after the washing methanol gas and filler in the packing layer;
(4) raw air is introduced in the superheater by the constant volume gas blower by air cleaning unit, the raw air import that enters the hot pressing pump after the heating again;
(5) in the hot pressing pump, have by the water vapor of center nozzle high-velocity jet, have, the raw air that is entered by air intlet is arranged by the methanol gas of peripheral spout high-velocity jet, three kinds of unstripped gases are taken out and are with the mixing back to flow to tail end by the diffuser tube of hot pressing pump, flow to superheater by mixed gas outlet again;
(6) through the cap of three kinds of mixing raw material gas flows of superheater superheated reactor, the catalyst layer that enters reactor that flows downward carries out oxidizing reaction generation formaldehyde gas, formaldehyde gas flows to the chilling tubulation district of reactor, by chilling tubulation one district, chilling tubulation two districts, after cooling off successively, chilling tubulation three districts enter the first grade absorption tower of reactor, in first grade absorption tower, entered condensation absorption formation formaldehyde liquid in the packing layer after the built-in water cooler cooling, the absorption that circulates of most of formaldehyde liquid, increase the liquid part as the finished product extraction, nonabsorbable formaldehyde gas recovering liquid after being absorbed by the multistage absorption tower is returned first grade absorption tower bottom, nonabsorbable exhaust emissions.
8. Formaldehyde Production technology according to claim 7, it is characterized in that the process that raw air enters the hot pressing pump is: raw air enters in the moistening packing layer of air scrubber behind the washing, purifying to be introduced in the superheater by the constant volume gas blower and heats, the air of emptying then still is back to the air washing tower bottom and participates in washing process, washings in the packing layer is the liquid distributor liquid of ejection downwards, this liquid is supplied with by circulating liquid, insufficient part or the liquid when just having started equipment derive from additional washings, are entered in the hot pressing pump by the air intlet of hot pressing pump by the superheater superheated air that comes out again.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011201894A CN1137074C (en) | 2001-07-11 | 2001-07-11 | Producing equipment for formaldehyde and its completed production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011201894A CN1137074C (en) | 2001-07-11 | 2001-07-11 | Producing equipment for formaldehyde and its completed production process |
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| CN1326918A true CN1326918A (en) | 2001-12-19 |
| CN1137074C CN1137074C (en) | 2004-02-04 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNB011201894A Expired - Fee Related CN1137074C (en) | 2001-07-11 | 2001-07-11 | Producing equipment for formaldehyde and its completed production process |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101239893B (en) * | 2007-02-05 | 2010-12-22 | 永港伟方（北京）科技股份有限公司 | Formaldehyde oxidation reactor |
| CN101486633B (en) * | 2009-02-11 | 2012-04-18 | 王承信 | Formaldehyde absorbing tower |
| CN101671239B (en) * | 2009-10-14 | 2012-11-07 | 江阴市华燕石化机械装备有限公司 | Double circulation system and double circulation process for preparing formaldehyde |
| CN103086854A (en) * | 2013-02-26 | 2013-05-08 | 河北凯跃化工集团有限公司 | Method and device for reducing methanol content in formaldehyde process by silver method |
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| CN103706303A (en) * | 2013-12-12 | 2014-04-09 | 桂林华德机械设备有限公司 | Novel formaldehyde oxidizer |
| CN109574820A (en) * | 2018-12-10 | 2019-04-05 | 安徽金禾实业股份有限公司 | A kind of production method of formaldehyde |
| CN110902653A (en) * | 2019-12-28 | 2020-03-24 | 上海华林工业气体有限公司 | Method for switching raw material crude CO into synthesis gas by synthesis gas separation device without stopping |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101239894B (en) * | 2007-02-05 | 2011-03-23 | 永港伟方（北京）科技股份有限公司 | Formaldehyde oxidation reactor |
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2001
- 2001-07-11 CN CNB011201894A patent/CN1137074C/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101239893B (en) * | 2007-02-05 | 2010-12-22 | 永港伟方（北京）科技股份有限公司 | Formaldehyde oxidation reactor |
| CN101486633B (en) * | 2009-02-11 | 2012-04-18 | 王承信 | Formaldehyde absorbing tower |
| CN101671239B (en) * | 2009-10-14 | 2012-11-07 | 江阴市华燕石化机械装备有限公司 | Double circulation system and double circulation process for preparing formaldehyde |
| CN103086854A (en) * | 2013-02-26 | 2013-05-08 | 河北凯跃化工集团有限公司 | Method and device for reducing methanol content in formaldehyde process by silver method |
| CN103086854B (en) * | 2013-02-26 | 2015-05-13 | 河北凯跃化工集团有限公司 | Method and device for reducing methanol content in formaldehyde process by silver method |
| CN103113201A (en) * | 2013-03-12 | 2013-05-22 | 江苏凯茂石化科技有限公司 | Production process of acetaldehyde |
| CN103706303A (en) * | 2013-12-12 | 2014-04-09 | 桂林华德机械设备有限公司 | Novel formaldehyde oxidizer |
| CN109574820A (en) * | 2018-12-10 | 2019-04-05 | 安徽金禾实业股份有限公司 | A kind of production method of formaldehyde |
| CN109574820B (en) * | 2018-12-10 | 2021-12-21 | 安徽金禾实业股份有限公司 | Production method of formaldehyde |
| CN110902653A (en) * | 2019-12-28 | 2020-03-24 | 上海华林工业气体有限公司 | Method for switching raw material crude CO into synthesis gas by synthesis gas separation device without stopping |
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| Publication number | Publication date |
|---|---|
| CN1137074C (en) | 2004-02-04 |
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