CN104815545A - Real-time desulfurizing agent and by product flow calculation method for wet desulphurization system - Google Patents

Abstract

The invention discloses a real-time desulfurizing agent and by product flow calculation method for a wet desulphurization system. According to the method, flue gas desulphurization (FGD) tower inlet work condition SO2 concentration SO [2] [fgdIn], FGD tower inlet glue gas V [yan, fgdIn] produced in each kilogram coal work condition, FGD tower outlet work condition SO2 concentration SO [2] [fgdOut], FGD tower outlet glue gas V [yan, fgdOut] produced in each kilogram coal work condition, fired coal real-time caloric value Qar and generator set active power Ne and power generation coal consumption Bf are subjected to real-time calculation to obtain the desulfurizing agent and by product flow of the wet desulphurization system. The basis for desulfurizing agent and by product calculation is provided by obtaining the desulfurizing agent and by product flow through calculation.

Description

A kind of method of real-time calculating wet desulfurization system desulfurizing agent and byproduct flow

Technical field:

The present invention relates to the fields such as heat energy, chemistry, information technology, be specifically related to a kind of method of real-time calculating wet desulfurization system desulfurizing agent and byproduct flow.

Background technology:

At present, thermal power plant's lime stone (lime)-gypsum wet desulphurization system sorbent consumption amount adopts the method for belt conveyer scale or coal powder silo with level meter, and its accuracy and real-time are difficult to ensure, and gypsum limits due to production technology, measures difficulty in real time larger.

Summary of the invention:

The object of the present invention is to provide a kind of method of real-time calculating wet desulfurization system desulfurizing agent and byproduct flow, utilize FGD absorption tower entrance condition condition SO ₂concentration SO2 _fgdIn, the flue gas volume V that produces of FGD absorption tower entrance every kilogram of coal working condition _{yan, fgdIn}, FGD absorption tower outlet condition condition SO ₂concentration SO2 _fgdOut, FGD absorption tower exports the flue gas volume V that every kilogram of coal working condition produces _{yan, fgdOut}, the real-time calorific value Q of as-fired coal _ar, generating set active power N _eand unit generation coal consumption B _f, calculate sorbent consumption amount and byproduct generation in real time, for sorbent consumption amount and byproduct generation statistics provide foundation.

For achieving the above object, the present invention adopts following technical scheme to be achieved:

A method for real-time calculating wet desulfurization system desulfurizing agent and byproduct flow, gathers FGD absorption tower entrance condition condition SO ₂concentration SO _2fgdIn, the flue gas volume V that produces of FGD absorption tower entrance every kilogram of coal working condition _{yan, fgdIn}, FGD absorption tower outlet condition condition SO ₂concentration SO _2fgdOut, FGD absorption tower exports the flue gas volume V that every kilogram of coal working condition produces _{yan, fgdOut}, the real-time calorific value Q of as-fired coal _ar, generating set active power N _eand unit generation coal consumption B _f, utilizing formula (1) to obtain take lime stone as the real-time traffic of desulfurizing agent:

${\mathrm{CaCO}}_3\left(m\right)=45.794\×{10}^{-6}\×\frac{N_e\×B_f}{Q_{\mathrm{ar}}}\×(V_{\mathrm{yan},\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{\mathrm{yan},\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{{\mathrm{CaCO}}_3}}---\left(1\right)$

In formula: N _e---generating set active power, MW;

B _f---the real-time gross coal consumption rate of unit, g/kWh;

V _{yan, fgdIn}---the flue gas volume that entrance every kilogram of coal working condition in FGD absorption tower produces, m ³/ kg;

V _{yan, fgdOut}---FGD absorption tower exports the flue gas volume that every kilogram of coal working condition produces, m ³/ kg;

SO _2fgdIn---FGD absorption tower entrance condition condition SO ₂concentration, mg/m ³;

SO _2fgdOut---FGD absorption tower outlet condition condition SO ₂concentration, mg/m ³;

Q _ar---the real-time calorific value of as-fired coal, kJ/kg;

Ca/S---calcium to sulphur mole ratio ,/;

---lime stone purity ,/;

CaCO ₃(m)---the real-time calculated mass flow of lime stone, t/h;

Utilizing formula (2) to obtain take lime as the real-time traffic of desulfurizing agent:

$\mathrm{CaO}\left(m\right)=25.665\×{10}^{-6}\×\frac{N_e\×B_f}{Q_{\mathrm{ar}}}\×(V_{\mathrm{yan},\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{\mathrm{yan},\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{\mathrm{CaO}}}---\left(2\right)$

In formula: η _caO---lime purity ,/;

CaO (m)---the real-time calculated mass flow of lime, t/h;

Formula (3) is utilized to obtain desulfuration byproduct real-time traffic:

${\mathrm{CaSO}}_4\·{2H}_{2}O\left(m\right)=78.765\×{10}^{-6}\×\frac{N_e\×B_f}{Q_{\mathrm{ar}}}\×(V_{\mathrm{yan},\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{\mathrm{yan},\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})/{\mathrm{\η}}_{\mathrm{sg}}---\left(3\right)$

In formula: η _sg---gypsum purity ,/;

CaSO ₄2H ₂o (m)---the plaster of paris calculates generation, t/h.

The present invention further improves and is,

When gateway, FGD absorption tower have the real-time measuring point of flue gas total flow or by the total flue gas flow calculated can meet precision be greater than 95% time, then:

Utilizing formula (4) to obtain take lime stone as the real-time traffic of desulfurizing agent:

${\mathrm{CaCO}}_3\left(m\right)=1.562\×{10}^{-3}\×\frac{(V_{Y,\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{Y,\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})}{{\mathrm{\η}}_{{\mathrm{NH}}_3}}\×\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{{\mathrm{CaCO}}_3}}---\left(4\right)$

Utilizing formula (5) to obtain take lime as the real-time traffic of desulfurizing agent:

$\mathrm{CaO}\left(m\right)=8.75\×{10}^{-4}\×\frac{(V_{Y,\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{Y,\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})}{{\mathrm{\η}}_{{\mathrm{NH}}_3}}\×\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{\mathrm{CaO}}}---\left(5\right)$

Formula (6) is utilized to obtain desulfuration byproduct real-time traffic:

CaSO ₄·2H ₂O(m)＝2.688×10 ^-3×(V _Y,fgdIn×SO _2fgdIn-V _Y,fgdOut×SO _2fgdOut)/η _sg(6)

In formula: V _{y, fgdIn}---porch, FGD absorption tower flue gas volume flow, km ³/ h;

V _{y, fgdOut}---exit, FGD absorption tower flue gas volume flow, km ³/ h.

Relative to prior art, the present invention has the following advantages: a kind of method of real-time calculating wet desulfurization system desulfurizing agent and byproduct flow, utilizes FGD absorption tower entrance condition condition SO ₂concentration SO _2fgdIn, the flue gas volume V that produces of FGD absorption tower entrance every kilogram of coal working condition _{yan, fgdIn}, FGD absorption tower outlet condition condition SO ₂concentration SO _2fgdOut, FGD absorption tower exports the flue gas volume V that every kilogram of coal working condition produces _{yan, fgdOut}, the real-time calorific value Q of as-fired coal _ar, generating set active power N _eand unit generation coal consumption B _f, calculate the real-time consumption of desulfurizing agent and byproduct generation in real time; Result of calculation of the present invention may be used for desulfurizing agent, byproduct statistics provides a kind of method; Realization of the present invention obtains the real-time generation of desulfuration byproduct first.

Detailed description of the invention:

The method of a kind of real-time calculating wet desulfurization system desulfurizing agent of the present invention and byproduct flow, gathers FGD absorption tower entrance condition condition SO ₂concentration SO _2fgdIn, the flue gas volume V that produces of FGD absorption tower entrance every kilogram of coal working condition _{yan, fgdIn}, FGD absorption tower outlet condition condition SO ₂concentration SO _2fgdOut, FGD absorption tower exports the flue gas volume V that every kilogram of coal working condition produces _{yan, fgdOut}, the real-time calorific value Q of as-fired coal _ar, generating set active power N _eand unit generation coal consumption B _f, calculate desulfurizing agent flow in real time.

1) lime stone flow rate calculation

Utilizing formula (1) to obtain take lime stone as the real-time traffic of desulfurizing agent:

${\mathrm{CaCO}}_3\left(m\right)=45.794\×{10}^{-6}\×\frac{N_e\×B_f}{Q_{\mathrm{ar}}}\×(V_{\mathrm{yan},\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{\mathrm{yan},\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{{\mathrm{CaCO}}_3}}---\left(1\right)$

In formula: N _e---generating set active power, MW;

B _f---the real-time gross coal consumption rate of unit, g/kWh;

V _{yan, fgdIn}---the flue gas volume that entrance every kilogram of coal working condition in FGD absorption tower produces, m ³/ kg;

V _{yan, fgdOut}---FGD absorption tower exports the flue gas volume that every kilogram of coal working condition produces, m ³/ kg;

SO _2fgdIn---FGD absorption tower entrance condition condition SO ₂concentration, mg/m ³;

SO _2fgdOut---FGD absorption tower outlet condition condition SO ₂concentration, mg/m ³;

Q _ar---the real-time calorific value of as-fired coal, kJ/kg;

Ca/S---calcium to sulphur mole ratio ,/;

η _caCO3---lime stone purity ,/;

CaCo ₃(m)---the real-time calculated mass flow of lime stone, t/h;

2) lime flow rate calculation

Utilizing formula (2) to obtain take lime as the real-time traffic of desulfurizing agent:

$\mathrm{CaO}\left(m\right)=25.665\×{10}^{-6}\×\frac{N_e\×B_f}{Q_{\mathrm{ar}}}\×(V_{\mathrm{yan},\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{\mathrm{yan},\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{\mathrm{CaO}}}---\left(2\right)$

In formula: η _caO---lime purity ,/;

CaO (m)---the real-time calculated mass flow of lime, t/h;

3) gypsum generation calculates

Formula (3) is utilized to obtain desulfuration byproduct gypsum real-time traffic:

${\mathrm{CaSO}}_4\·{2H}_{2}O\left(m\right)=78.765\×{10}^{-6}\×\frac{N_e\×B_f}{Q_{\mathrm{ar}}}\×(V_{\mathrm{yan},\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{\mathrm{yan},\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})/{\mathrm{\η}}_{\mathrm{sg}}---\left(3\right)$

In formula: η _sg---gypsum purity ,/;

CaSO ₄2H ₂o (m)---the plaster of paris calculates generation, t/h;

4) related description

In view of SO ₂real-time concentration is measured under being working condition, therefore with V in above formula (1), formula (2), formula (3) _{yan, fgdIn}, V _{yan, fgdOut}the dry flue gas volume flow produced by every kilogram of coal mark condition condition, inleakage and water vapour content three sum, then be converted to the flue gas volume under working condition, its specific algorithm can with reference to fired coal combustion equation and exhaust gas volumn calculating etc.

When gateway, FGD absorption tower have the real-time measuring point of flue gas total flow or by the total flue gas flow calculated can meet precision be greater than 95% time, then:

Lime stone mass flow calculation can adopt:

${\mathrm{CaCO}}_3\left(m\right)=1.562\×{10}^{-3}\×\frac{(V_{Y,\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{Y,\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})}{{\mathrm{\η}}_{{\mathrm{NH}}_3}}\×\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{{\mathrm{CaCO}}_3}}---\left(4\right)$

Lime quality flow rate calculation can adopt:

$\mathrm{CaO}\left(m\right)=8.75\×{10}^{-4}\×\frac{(V_{Y,\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{Y,\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})}{{\mathrm{\η}}_{{\mathrm{NH}}_3}}\×\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{\mathrm{CaO}}}---\left(5\right)$

Plaster of paris mass flow calculation can adopt:

CaSO ₄·2H ₂O(m)＝2.688×10 ^-3×(V _Y,fgdIn×SO _2fgdIn-V _Y,fgdOut×SO _2fgdOut)/η _sg(6)

In formula: V _{y, fgdIn}---porch, FGD absorption tower flue gas volume flow, km ³/ h;

V _{y, fgdOut}---exit, FGD absorption tower flue gas volume flow, km ³/ h.

5) stability calculated and accuracy

In order to ensure the accurately fixed of result of calculation and stability, FGD absorption tower entrance condition condition SO ₂concentration, FGD absorption tower outlet condition condition SO ₂the real time datas such as the real-time gross coal consumption rate of concentration, unit, the real-time calorific value of as-fired coal adopt the mean value in certain hour to calculate, and Real-time Collection needs verification, then substitutes into formulae discovery.Real-time result of calculation may be used for being analyzed with measured data and providing a kind of method for grasping FGD system byproduct real-time traffic.

Claims (2)

1. calculate a method for wet desulfurization system desulfurizing agent and byproduct flow in real time, it is characterized in that, gather FGD absorption tower entrance condition condition SO ₂concentration SO _2fgdIn, the flue gas volume V that produces of FGD absorption tower entrance every kilogram of coal working condition _{yan, fgdIn}, FGD absorption tower outlet condition condition SO ₂concentration SO _2fgdOut, FGD absorption tower exports the flue gas volume V that every kilogram of coal working condition produces _{yan, fgdOut}, the real-time calorific value Q of as-fired coal _ar, generating set active power N _eand unit generation coal consumption B _f, utilizing formula (1) to obtain take lime stone as the real-time traffic of desulfurizing agent:

${\mathrm{CaCO}}_3\left(m\right)=45.797\×{10}^{-6}\×\frac{N_e\×B_f}{Q_{\mathrm{ar}}}\×(V_{\mathrm{yan},\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{\mathrm{yan},\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{\mathrm{CaC}{O}_3}}---\left(1\right)$

In formula: N _e---generating set active power, MW;

B _f---the real-time gross coal consumption rate of unit, g/kWh;

V _{yan, fgdIn}---the flue gas volume that entrance every kilogram of coal working condition in FGD absorption tower produces, m ³/ kg;

V _{yan, fgdOut}---FGD absorption tower exports the flue gas volume that every kilogram of coal working condition produces, m ³/ kg;

SO _2fgdIn---FGD absorption tower entrance condition condition SO ₂concentration, mg/m ³;

SO _2fgdOut---FGD absorption tower outlet condition condition SO ₂concentration, mg/m ³;

Q _ar---the real-time calorific value of as-fired coal, kJ/kg;

Ca/S---calcium to sulphur mole ratio ,/;

---lime stone purity ,/;

CaCO ₃(m)---the real-time calculated mass flow of lime stone, t/h;

Utilizing formula (2) to obtain take lime as the real-time traffic of desulfurizing agent:

$\mathrm{CaO}\left(m\right)=25.665\×{10}^{-6}\×\frac{N_e\×B_f}{Q_{\mathrm{ar}}}\×(V_{\mathrm{yan},\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{\mathrm{yan},\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})\×\frac{\mathrm{Ca}/S}{{\mathrm{\η}}_{\mathrm{CaO}}}---\left(2\right)$

In formula: η _caO---lime purity ,/;

CaO (m)---the real-time calculated mass flow of lime, t/h;

Formula (3) is utilized to obtain desulfuration byproduct real-time traffic:

${\mathrm{CaSO}}_4\·2H_{2}O\left(m\right)=78.765\×{10}^{-6}\×\frac{N_e\×B_f}{Q_{\mathrm{ar}}}\×(V_{\mathrm{yan},\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{\mathrm{yan},\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})/{\mathrm{\η}}_{\mathrm{sg}}---\left(3\right)$

In formula: η _sg---gypsum purity ,/;

CaSO ₄2H ₂o (m)---the plaster of paris calculates generation, t/h.

2. the method for a kind of real-time calculating wet desulfurization system desulfurizing agent according to claim 1 and byproduct flow, is characterized in that,

When gateway, FGD absorption tower have the real-time measuring point of flue gas total flow or by the total flue gas flow calculated can meet precision be greater than 95% time, then:

Utilizing formula (4) to obtain take lime stone as the real-time traffic of desulfurizing agent:

${\mathrm{CaCO}}_3\left(m\right)=1.562\×{10}^{-3}\×\frac{(V_{Y,\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{Y,\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})}{{\mathrm{\η}}_{{\mathrm{NH}}_3}}\×\×\frac{\mathrm{Ca}/s}{{\mathrm{\η}}_{{\mathrm{CaCO}}_3}}---\left(4\right)$

Utilizing formula (5) to obtain take lime as the real-time traffic of desulfurizing agent:

$\mathrm{CaO}\left(m\right)=8.75\×{10}^{-4}\×\frac{(V_{Y,\mathrm{fgdIn}}\×{\mathrm{SO}}_{2\mathrm{fgdIn}}-V_{Y,\mathrm{fgdOut}}\×{\mathrm{SO}}_{2\mathrm{fgdOut}})}{{\mathrm{\η}}_{{\mathrm{NH}}_3}}\×\×\frac{\mathrm{Ca}/s}{{\mathrm{\η}}_{\mathrm{CaO}}}---\left(5\right)$

Formula (6) is utilized to obtain desulfuration byproduct real-time traffic:

CaSO ₄·2H ₂O(m)＝2.688×10 ^-3×(V _Y,fgdIn×SO _2fgdIn-V _Y,fgdOut×SO _2fgdOut)/η _sg(6)

In formula: V _{y, fgdIn}---porch, FGD absorption tower flue gas volume flow, km ³/ h;

V _{y, fgdOut}---exit, FGD absorption tower flue gas volume flow, km ³/ h.