CN101284651A - Method for conveying crude product of thionyl chloride form low pressure to high pressure by high potential difference - Google Patents
Method for conveying crude product of thionyl chloride form low pressure to high pressure by high potential difference Download PDFInfo
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- CN101284651A CN101284651A CNA2008100011960A CN200810001196A CN101284651A CN 101284651 A CN101284651 A CN 101284651A CN A2008100011960 A CNA2008100011960 A CN A2008100011960A CN 200810001196 A CN200810001196 A CN 200810001196A CN 101284651 A CN101284651 A CN 101284651A
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Abstract
The invention provides a method that transports a crude product of thionyl chloride from low pressure to high pressure by utilizing a high potential difference. The method consists of the following steps: forming a pressure difference by taking advantage of the high and the low position differences among a thionyl chloride reaction kettle, a condenser of the crude product of thionyl chloride, and a degassing device of the crude product of thionyl chloride, and at the same time arranging a U-shaped pipe that is taken as a liquid seal between the crude product condenser and the degassing device, thereby finishing the transportation of a gaseous or liquid crude product of thionyl chloride wihtout using pumps. By adopting the method, a plurality of pumps used for transporting raw materials are reduced, and more importantly, as the pumps used for transporting the raw materials are reduced or not used, the possibility of overflow of the reaction materials can be reduced in the maximal degree, the possibility of environmental pollution caused by the reaction materials is reduced, the recycling use of residual materials is greatly improved, and the utilization ratio of the material is improved.
Description
Invention field
The present invention relates to be a kind of utilize high potential difference make the crude product sulfur oxychloride from low-pressure delivery to the highly compressed method, concretely, what the present invention relates to is that a kind of position of sulfur oxychloride synthesis reactor, crude product sulfur oxychloride condenser and crude product sulfur oxychloride de-gassing vessel that utilizes just forms pressure reduction, simultaneously a U type pipe is set between crude product condenser and de-gassing vessel, thereby under the situation of not utilizing pump, finishes the conveying of gaseous state or liquid sulfur oxychloride crude product as fluid-tight.
Background technology
Sulfur oxychloride is dissolved in benzene, chloroform and tetracol phenixin, in water, decompose and generate sulfurous acid and hydrogenchloride, be heated to 140 degree and decompose generation chlorine, sulfurous gas and sulfur monochloride, the chlorine atom substituted hydroxy of sulfur oxychloride and sulfydryl very capable, sometimes also can replace sulfurous gas, oxygen or hydrogen, can generate the corresponding chlorinated thing with organic compound reactions such as phenol that hydroxyl is arranged or alcohol, generate SULPHURYL CHLORIDE with the sulfonic acid reaction, the sharp refined reagent react of dative generates corresponding sulfoxide compound etc.Sulfur oxychloride is very important in organic synthesis, and it is agricultural chemicals, medicine, sensitive materials and superpolymer intermediate synthetic intermediate raw material, and prior art discloses the technical scheme of synthesizing, purifying of some sulfur oxychlorides, comprising:
ZL95110380 discloses a kind of manufacture method of sulfur oxychloride, this method is to utilize the monochloride of sulfurous gas with sulfur subchloride, dichloride with gac as making the sulfur oxychloride crude product with gas-phase reaction in the presence of the catalyzer, again crude product and SULPHUR POWDER are distilled together and make elaboration, concrete reactions steps has the synthetic of disulphur dichloride, synthesizing of sulfur dichloride, the purification of the synthetic and crude product of sulfur oxychloride, but, the described intermittent mode of production of this patent, because polystep reaction wherein is reversible reaction, therefore, in order to realize the complete of forward reaction, the part starting raw material that needs volume, the great difficulty that has caused the reaction back to be reclaimed, simultaneously, the utilization ratio of raw materials of the described technology of this patent only can improve more than 50 percent, and yield also improves 50 percent than prior art.
US2431823 discloses and has utilized disulphur dichloride (S
2Cl
2) and chlorine reaction, the sulfur dichloride (SCl of generation
2) and excessive chlorine and chlorine gas-phase reaction under activated carbon catalysis of sulfurous gas and importing, obtain sulfur oxychloride through distillation; The document also discloses that will reaction after the being mainly sulfur monochloride mixture that comprises sulphur after over cure bed and the distillation adds preheater A after through the chlorinator chlorination, begin new reaction.
US2,779,663 disclose acquisition SOCl
2Method, comprise the degassing (sulfurous gas and chlorine), condensation, mention S in the background technology
2Cl
2, SO
2And Cl
2Reaction generates SOCl
2, and the sulfur dichloride reaction that product will be wherein in vulcanizing apparatus is sulfur monochloride, turn back to the reactor of beginning; The reactor that sulfurous gas that reclaims and chlorine turn back to beginning.
The document that directly relates to the synthesizing chlorinated sulfoxide of sulfurous gas gas phase method has: US2431823, DE842041;
Be that the document that initiator produces the synthesizing chlorinated sulfoxide of sulfur monochloride has US1861900, US2420623 with sulphur;
In sum, in the prior art, the method for synthesizing chlorinated sulfoxide has tens kinds, and still, large-scale industrial production is following three kinds of operational paths basically:
(1) phosphorus pentachloride and sulfurous gas reaction, technology is simple, but SOCl
2With POCl
3Be difficult to separate, be difficult to obtain high purity SOCl
2
(2) be catalyzer with antimony chloride etc., sulfur subchloride and chlorsulfonic acid reaction, domestic extensive employing at present, complex process is invested bigger;
(3) the synthesizing chlorinated sulfoxide of gas-phase catalysis is a catalyzer with the gac, sulfur subchloride and sulfurous gas, chlorine reaction, abroad generally adopt, technology is simple, less investment and product purity height, can adopt closed internal circulation apparatus production, non-environmental-pollution, the primitive reaction formula is as follows:
(1)、
(2)、
But, in disclosed document,, adopt closed internal recycle method to produce though proposition is arranged,, as a heavy construction project, not open how closed internal recycle method is produced the concrete technical scheme of sulfur oxychloride, in view of this, specially proposes the present invention.
Goal of the invention
The object of the present invention is to provide a kind of high potential difference that utilizes to make condensed crude product sulfur oxychloride be transported to the method the crude product de-gassing vessel in relatively high pressure interval from the relatively low pressure interval.
Purpose of the present invention can be achieved in the following manner: what the present invention relates to is that a kind of utilization utilizes the position of sulfur oxychloride synthesis reactor, crude product sulfur oxychloride condenser and crude product sulfur oxychloride de-gassing vessel just to form pressure reduction, simultaneously a U type pipe is set between crude product condenser and de-gassing vessel, thereby under the situation of not utilizing pump, finishes the conveying of gaseous state or liquid sulfur oxychloride crude product as fluid-tight.
A kind of crude product sulfur oxychloride carrying method provided by the invention, wherein the synthetic method of sulfur oxychloride comprises the synthetic of sulfur oxychloride, the condensation and the degassing, respectively at the sulfur oxychloride synthesis reactor, carry out in crude product sulfur oxychloride condenser and the crude product sulfur oxychloride de-gassing vessel, crude product sulfur oxychloride synthesis reactor is connected with crude product sulfur oxychloride condenser, crude product sulfur oxychloride condenser is connected with crude product sulfur oxychloride de-gassing vessel again, and the discharge port level height that it is characterized in that crude product sulfur oxychloride condenser is arranged on the liquid level height of sulfur oxychloride liquid form mixt of crude product sulfur oxychloride de-gassing vessel.
Best, the discharge port level height of crude product sulfur oxychloride condenser is arranged on the level height of opening for feed of crude product sulfur oxychloride de-gassing vessel; Preferably, the discharge port level height of crude product sulfur oxychloride condenser is arranged on the level height of opening for feed of crude product sulfur oxychloride de-gassing vessel, the about 1-5 rice of the high potential difference between them; Most preferred, the discharge port level height of crude product sulfur oxychloride condenser is arranged on the level height of opening for feed of crude product sulfur oxychloride de-gassing vessel, the about 2.8-3.2 rice of the high potential difference between them.
The discharge port of crude product sulfur oxychloride condenser and and the opening for feed of crude product sulfur oxychloride de-gassing vessel between be provided with one and form " U " pipe of fluid-tight or similar liquid seal device, the interior pressure of described crude product sulfur oxychloride condenser is less than the interior pressure 0.01-0.04Mpa of crude product sulfur oxychloride de-gassing vessel, and described fluid-tight can prevent that gas from flowing back to the crude product condenser from the higher crude product degassing still of interior pressure.
Utilizing the pressure reduction that forms between crude product sulfur oxychloride condenser and the crude product sulfur oxychloride de-gassing vessel that the crude product sulfur oxychloride of liquid state is transported to the crude product de-gassing vessel from the condenser discharge port outgases, regulate to press in the crude product de-gassing vessel making it greater than the interior pressure of sulfur oxychloride synthesis reactor so that make the gas flow sulfur oxychloride synthesis reactor circulating reaction deviate from the degassing still simultaneously, synthetic gaseous state crude product sulfur oxychloride is delivered to crude product sulfur oxychloride condenser in the sulfur oxychloride synthesis reactor under pressure-driven.
The adjusting of pressing in the crude product de-gassing vessel be that what that utilize material in the crude product de-gassing vessel are regulated or the crude product de-gassing vessel in the adjustings of pressing be that to utilize the adjusting of pressing in that crude product de-gassing vessel Heating temperature is regulated or the crude product de-gassing vessel be to utilize the height of what and temperature of material in the crude product de-gassing vessel to regulate simultaneously.
The unnecessary gas of crude product condenser can utilize pump to pump in the synthesis reactor.
Pressure in the crude product condenser is about 0.02～0.23MPa, and pressure is 0.03～0.30Mpa in the de-gassing vessel.
Pressure reduction≤the 0.04Mpa that forms between crude product condenser and the crude product de-gassing vessel.
Concrete summary of the invention
In the present invention, for technical scheme of the present invention is described, part of compounds synthetic made following description:
The chemical equation of synthesizing chlorinated sulfoxide is as follows in the prior art, that is:
1, synthetic sulfur monochloride (S
2Cl
2)
The fusing point of sulphur is 112.8 ℃;
Disulphur dichloride (sulfur subchloride, sulfur monochloride) is a kind of colourless or orange-yellow oily liquid, and pungent odour is arranged, molecular weight 135.02, relative density 1.678, fusing point-80 ℃, 138 ℃ of boiling points, English name: Sulfur monochloride, molecular formula: S
2Cl
2
Chemical equation: 2S+Cl
2→ S
2Cl
2+ Q Q=58.1KJ/mol;
Reaction principle: the synthetic sulfur monochloride of the directly logical chlorine chlorination of powdery sulphur, reaction process is emitted heat.70～80 ℃ of temperature of reaction.
2, synthetic sulfur dichloride (SCl
2)
Sulfur dichloride is a kind of reddish-brown liquid, and pungent odour is arranged, molecular weight 103.02, and relative density 1.638 is heated and is decomposed more than 40 ℃, English name: Sulfur dichloride, molecular formula: SCl
2
Chemical equation: S
2Cl
2+ Cl
2→ 2SCl
2
Reaction principle: the further chlorination of the excessive logical chlorine of sulfur monochloride generates sulfur dichloride.65～85 ℃ of temperature of reaction;
3, synthesizing chlorinated sulfoxide (SOCl
2)
Sulfur oxychloride has another name called thionyl chloride, sulfurous oxychloride, and outward appearance is colourless or light yellow transparent liquid, and the strong impulse smell is arranged, and molecular formula is SOCl
2, molecular weight is 118.97, fusing point-105 ℃, 78.8 ℃ of boiling points, relative density 1.676g/m
3(20 ℃).
Reaction equation:
Cl
2+S
2Cl
2→2SCl
2
SCl
2+Cl
2+SO
2→2SOCl
2
Pay reaction: SO
2+ Cl
2→ SO
2Cl
2(SULPHURYL CHLORIDE)
This building-up reactions is carried out in the sulfur oxychloride synthesis reactor, and temperature of reaction is 200～250 ℃.
Reaction principle: SCl
2, Cl
2And SO
2Form mixed gas by a certain percentage.This gas mixture reacts on the activated-carbon catalyst surface, generates the crude product sulfur oxychloride.
In the present invention, SOCl
2Building-up reactions adopt no fixed carbon compositing catalyst.
4, sulfur oxychloride rectifying
Crude product SOCl
2In contain unreacted SCl
2, S
2Cl
2And be partly dissolved therein Cl
2And SO
2, rectifying is to utilize the different principle of each component relative volatility in the mixture, reaches the purpose of separating the purification sulfur oxychloride.
Rectifying is carried out in rectifying tower, and rectifying enters subsider with bottom product after finishing, and pumps into S then
2Cl
2Storage tank passes through S
2Cl
2Transferpump is delivered to S
2Cl
2Header tank, S
2Cl
2S in the header tank
2Cl
2Mixed solution is after the spinner-type flowmeter metering, quantitatively to SCl
2Synthetic SCl is made in the synthesis reactor charging
2Use, thereby finish the liquid phase circulation.
Wherein, synthetic sulfur oxychloride (SOCl in step 3 sulfur oxychloride synthesis reactor
2) be gaseous state crude product sulfur oxychloride, before rectifying, need through condensation liquefy crude product sulfur oxychloride, this step is carried out in crude product sulfur oxychloride condenser, there are a large amount of chlorine, sulfurous gas and sulfur dichloride to exist in the liquid crude product sulfur oxychloride, therefore remove chlorine and sulfurous gas by crude product sulfur oxychloride de-gassing vessel, chlorine of removing and sulfurous gas are circulated to and continue reaction in the sulfur oxychloride synthesis reactor, to increase raw material availability.The liquid crude product sulfur oxychloride of removing chlorine and sulfurous gas is passed in the crude product sulfur still, is dissolved in sulfur dichloride in the sulfur oxychloride and the solid sulphur of adding reacts at this, becomes high boiling sulfur monochloride, is beneficial to the carrying out of subsequent technique rectifying.
As outstanding feature of the present invention, in the synthesis technique of described sulfur oxychloride, utilize the position of sulfur oxychloride synthesis reactor, crude product sulfur oxychloride condenser and crude product sulfur oxychloride de-gassing vessel to form pressure reduction, simultaneously a U type pipe is set between crude product condenser and de-gassing vessel as fluid-tight, thereby under the situation of not utilizing pump, finish the conveying of gaseous state sulfur oxychloride, generally speaking, the de-gassing vessel degassing commonly used still.
Concrete, the discharge port level height of crude product sulfur oxychloride condenser of the present invention can be arranged on the liquid level height of sulfur oxychloride liquid form mixt of crude product sulfur oxychloride de-gassing vessel, such setting is exactly can utilize gravity to form pressure reduction between the two in order to make, so that the liquid in the condenser is pressed higher relatively de-gassing vessel in can flowing to.
General, in order to ensure forming clear and definite pressure reduction between described condenser and the de-gassing vessel, it is feasible that the clear and definite discharge port level height with the sulfur oxychloride condenser is arranged on the level height of opening for feed of crude product sulfur oxychloride de-gassing vessel, preferred scheme is about 1-5 rice on the level height of the discharge port level height of the condenser opening for feed that is arranged on the crude product de-gassing vessel, preferably, the about 2.8-3.2 rice of the high potential difference between them.
In order to prevent that the gas in the de-gassing vessel from flowing backward in the condenser, can the discharge port of crude product sulfur oxychloride condenser and and the opening for feed of crude product sulfur oxychloride de-gassing vessel between be provided with one and can form " U " pipe of fluid-tight or similar liquid seal device.
Similarly liquid seal device can be selected to use in the prior art, but, the present invention preferably can form " U " pipe of fluid-tight, and the pressure reduction that forms between described crude product sulfur oxychloride condenser and the crude product sulfur oxychloride de-gassing vessel is greater than the about 0.01-0.04Mpa of interior pressure of crude product sulfur oxychloride de-gassing vessel.
During use, the pressure reduction that forms between condenser and the crude product sulfur oxychloride de-gassing vessel is transported to the crude product de-gassing vessel with the crude product sulfur oxychloride of liquid state from the condenser discharge port and outgases, regulate simultaneously and press in the crude product de-gassing vessel greater than the interior pressure of sulfur oxychloride synthesis reactor so that make the gas flow sulfur oxychloride synthesis reactor circulating reaction deviate from the degassing still, synthetic gaseous state crude product sulfur oxychloride is delivered to crude product sulfur oxychloride condenser in the sulfur oxychloride synthesis reactor under pressure-driven.
The adjusting of pressing in the described crude product de-gassing vessel is to utilize the height of what and/or temperature of material in the crude product de-gassing vessel to regulate, and when the material in the discharging crude product de-gassing vessel was vacateed more spaces, pressure reduced, otherwise increases; Pressing in when improving the de-gassing vessel temperature increases, otherwise reduces.In fact, the interior pressure reduction of crude product condenser and de-gassing vessel is very little, is about 0.02Mpa, perhaps less than 0.01Mpa, or littler.The unnecessary gas of crude product condenser also can utilize pump to pump in the synthesis reactor.Generally speaking, pressure in the crude product condenser is about 0.02～0.23MPa, pressure is 0.03～0.30Mpa in the de-gassing vessel, the pressure reduction that forms between crude product condenser and the crude product de-gassing vessel is best≤and 0.04Mpa, the pressure in the sulfur oxychloride synthesis reactor is generally 0.12～0.13Mpa.
The invention has the beneficial effects as follows: the crude product sulfur oxychloride of liquid is utilized the crude product de-gassing vessel of gravity transfer to relatively high pressure from the condenser of relatively low pressure, so that the crude product de-gassing vessel of relatively high pressure forms higher relatively discharge port pressure, the gas of deviating from after the feasible heating participates in the gas phase of sulfur oxychloride and synthesizes, simultaneously, need not to be provided with in addition pump, utilize pressure reduction and/or the gravity sulfur oxychloride after the crude product sulfur still is carried degassing purification.
Adopt technology of the present invention, can reduce the various pumps that transferring raw material uses, more importantly be, owing to reducing or not using pump to come transferring raw material, can farthest reduce the possibility that reaction mass is overflowed, reduce the pollution of expecting and may and improve recycling of salvage stores, improved the utilization ratio of material environment.
Description of drawings
Fig. 1 is the preparation technology's of a sulfur oxychloride of the present invention basic flow sheet.
Fig. 2 is that the high potential difference that utilizes of the present invention makes the synoptic diagram of gas phase crude product sulfur oxychloride from low-pressure delivery to the highly compressed method.
In order to clearly demonstrate the present invention, special numbering with component names in the accompanying drawing and correspondence is listed sulfur dichloride synthesis reactor 1, sulfur oxychloride synthesis reactor 2, crude product condenser 3, degassing purification still 4, crude product sulfur still 5, rectifying condenser 6, rectifying tower 7, tower still 8, sulfur monochloride transferpump 9, crude product discharge port 10.
P1-P5 is the gaseous tension in each device.
Embodiment
Embodiment one
The synthesis technique of sulfur oxychloride and device are with reference to Fig. 1 and specification sheets part, the key of carrying method is, different with prior art, the sulfur oxychloride synthetic gas passes through pressure difference, after being transported to the crude product condenser condenses, the crude product phlegma enters by a fluid-tight and enters the operation that outgases of degassing still, and the gas of deviating from is delivered to the recycle of sulfur oxychloride synthesis reactor because of what pressure reduction was recycled again.Wherein the pressure in the condenser is 0.18MPa, and condensator outlet pressure is 0.18MPa, and pressure is 0.2MPa in the de-gassing vessel, and back pressure is 0.2MPa.High potential difference between crude product condenser and the de-gassing vessel is 3 meters.The gas that exports out from de-gassing vessel comprises sulfur dioxide gas and chlorine, reenters the sulfur oxychloride synthesis reactor, uses as the raw material continuation of synthesizing chlorinated sulfoxide.
Embodiment two
The synthesis technique of sulfur oxychloride and device are with reference to Fig. 1 and specification sheets part, crude product sulfur oxychloride liquid is delivered to from the condenser of relatively low pressure relatively high pressure the crude product de-gassing vessel in concentrate, wherein the pressure in the condenser is 0.2MPa, condensator outlet pressure is 0.2MPa, pressure is 0.22MPa in the de-gassing vessel, and back pressure is 0.22MPa.High potential difference between crude product condenser and the de-gassing vessel is 5 meters.The gas that exports out from de-gassing vessel comprises sulfur dioxide gas and chlorine, reenters the sulfur oxychloride synthesis reactor, uses as the raw material continuation of synthesizing chlorinated sulfoxide.
Embodiment three
The synthesis technique of sulfur oxychloride and device are with reference to Fig. 1 and specification sheets part, crude product sulfur oxychloride liquid is delivered to the crude product de-gassing vessel of relatively high pressure from the condenser of relatively low pressure, wherein the pressure in the condenser is 0.02MPa, condensator outlet pressure is 0.02MPa, pressure is 0.03MPa in the de-gassing vessel, and back pressure is that the high potential difference between 0.03MPa crude product condenser and the de-gassing vessel is 3 meters.
Embodiment four
The synthesis technique of sulfur oxychloride and device are with reference to Fig. 1 and specification sheets part, crude product sulfur oxychloride liquid is delivered to the crude product de-gassing vessel of relatively high pressure from the condenser of relatively low pressure, wherein the pressure in the condenser is 0.23MPa, condensator outlet pressure is 0.23MPa, pressure is 0.30MPa in the de-gassing vessel, and back pressure is that the high potential difference between 0.30MPa crude product condenser and the de-gassing vessel is 1 meter.
Embodiment five
The synthesis technique of sulfur oxychloride and device are with reference to Fig. 1 and specification sheets part, crude product sulfur oxychloride liquid is delivered to the crude product de-gassing vessel of relatively high pressure from the condenser of relatively low pressure, wherein the pressure in the condenser is 0.12MPa, condensator outlet pressure is 0.12MPa, pressure is 0.13MPa in the de-gassing vessel, and back pressure is that the high potential difference between 0.13MPa crude product condenser and the de-gassing vessel is 2.8 meters.
Embodiment six
The synthesis technique of sulfur oxychloride and device are with reference to Fig. 1 and specification sheets part, crude product sulfur oxychloride liquid is delivered to the crude product de-gassing vessel of relatively high pressure from the condenser of relatively low pressure, wherein the pressure in the condenser is 0.18MPa, condensator outlet pressure is 0.18MPa, pressure is 0.22MPa in the de-gassing vessel, and back pressure is 0.22MPa.High potential difference between crude product condenser and the de-gassing vessel is 3.2 meters.
Claims (10)
1, a kind of utilize high potential difference make the crude product sulfur oxychloride from low-pressure delivery to the highly compressed method, wherein the synthetic method of sulfur oxychloride comprises the synthetic of sulfur oxychloride, the condensation and the degassing, respectively at the sulfur oxychloride synthesis reactor, carry out in crude product sulfur oxychloride condenser and the crude product sulfur oxychloride de-gassing vessel, crude product sulfur oxychloride synthesis reactor is connected with crude product sulfur oxychloride condenser, crude product sulfur oxychloride condenser is connected with crude product sulfur oxychloride de-gassing vessel again, and the discharge port level height that it is characterized in that crude product sulfur oxychloride condenser is arranged on the liquid level height of sulfur oxychloride liquid form mixt of crude product sulfur oxychloride de-gassing vessel.
2, method according to claim 1, the discharge port level height that it is characterized in that crude product sulfur oxychloride condenser are arranged on the level height of opening for feed of crude product sulfur oxychloride de-gassing vessel; Preferably, the discharge port level height of crude product sulfur oxychloride condenser is arranged on the level height of opening for feed of crude product sulfur oxychloride de-gassing vessel, the high potential difference 1-5 rice between them; Best, the discharge port level height of crude product sulfur oxychloride condenser is arranged on the level height of opening for feed of crude product sulfur oxychloride de-gassing vessel, the high potential difference 2.8-3.2 rice between them.
3, method according to claim 1 and 2, it is characterized in that the discharge port of crude product sulfur oxychloride condenser and and the opening for feed of crude product sulfur oxychloride de-gassing vessel between be provided with one and form " U " pipe of fluid-tight or similar liquid seal device, the interior pressure of described crude product sulfur oxychloride condenser is less than the interior pressure 0.01-0.04Mpa of crude product sulfur oxychloride de-gassing vessel, and described fluid-tight can prevent that gas from flowing back to the crude product condenser from the higher crude product degassing still of interior pressure.
4, according to claim 1 or 2 or 3 described methods, it is characterized in that utilizing the pressure reduction that forms between crude product sulfur oxychloride condenser and the crude product sulfur oxychloride de-gassing vessel that the crude product sulfur oxychloride of liquid state is transported to the crude product de-gassing vessel from the condenser discharge port outgases, regulate to press in the crude product de-gassing vessel making it greater than the interior pressure of sulfur oxychloride synthesis reactor so that make the gas flow sulfur oxychloride synthesis reactor circulating reaction deviate from the degassing still simultaneously, synthetic gaseous state crude product sulfur oxychloride is delivered to crude product sulfur oxychloride condenser in the sulfur oxychloride synthesis reactor under pressure-driven.
5, method according to claim 4 is characterized in that the adjusting of pressing in the crude product de-gassing vessel is to utilize how many adjustings of material in the crude product de-gassing vessel.
6, method according to claim 4 is characterized in that the adjusting of pressing in the crude product de-gassing vessel utilizes crude product de-gassing vessel Heating temperature to regulate.
7, method according to claim 4 is characterized in that the adjusting of pressing in the crude product de-gassing vessel is to utilize the height adjusting of what and temperature of material in the crude product de-gassing vessel simultaneously.
8, method according to claim 1 is characterized in that the unnecessary gas of crude product condenser can utilize pump to pump in the synthesis reactor.
9, method according to claim 4 is characterized in that the pressure in the crude product condenser is 0.02～0.23MPa, and pressure is 0.03～0.30Mpa in the de-gassing vessel.
10, method according to claim 4 is characterized in that the pressure reduction≤0.04Mpa that forms between crude product condenser and the crude product de-gassing vessel.
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|---|---|---|---|
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|---|---|---|---|
| CNB2008100011960A CN100480172C (en) | 2008-01-18 | 2008-01-18 | Method for conveying crude product of thionyl chloride form low pressure to high pressure by high potential difference |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105330500A (en) * | 2015-12-14 | 2016-02-17 | 山东凯盛新材料有限公司 | Continuous production method of aromatic acyl chloride |
| CN115672217A (en) * | 2022-10-27 | 2023-02-03 | 莒南国泰化工有限公司 | Device and method for improving yield of thionyl chloride |
-
2008
- 2008-01-18 CN CNB2008100011960A patent/CN100480172C/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105330500A (en) * | 2015-12-14 | 2016-02-17 | 山东凯盛新材料有限公司 | Continuous production method of aromatic acyl chloride |
| CN115672217A (en) * | 2022-10-27 | 2023-02-03 | 莒南国泰化工有限公司 | Device and method for improving yield of thionyl chloride |
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| Publication number | Publication date |
|---|---|
| CN100480172C (en) | 2009-04-22 |
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